r 


J&IMM  ffll  w 


UNION 

ENGINEERING 

HANDBOOK 


TUMPING  MACHINERY 
COMPRESSORS 
CONDENSERS 


COMPILED    BY 

E.  P.  ORDWAY,  M.  E. 


SIXTH  EDITION 


PRICE   $5.OO 

UNION  STEAM  PUMP  CO. 

BATTLE  CREEK,    MICHIGAN 
U.  S.  A. 


PRINTED  IN  THE  U,  S.  A. 


TT16Q 
0' 


COPYRIGHT.     1821, 
BY  THE 

UNION    STEAM      PUMP   COMPANY 

BATTLE  CREEK.  MICHIGAN 

U.    S,    A. 


ELL-IS   PUBLISHING   CO. 

PRINTERS.   ENGRAVERS 

ELECTROTYPERS,  BINDERS 

AND  RULERS 

BATTLE  CREEK,  MICHIGAN 


BATTLE      CREEK.     MICHIGAN.      U.S.A. 


I! 


INDEX 


Accessories,  Electrical 252-255 

Accumulators 341 

Acid  Sludge  Pumps -  474 

Actual  Compression  with  Clearance.- 8 

Adiabatic  Compression.— 4 

Advantages  of  Centrifugal  Pumps 97 

Advantages- of  Different  Types  of  Drives  for  Power  Pumps 382 

Advantages  of  Duplex  Pumps 266 

Advantages  of  Multistage  Compression 12 

Advantages  of  Single  Pumps 263 

Air  Chambers,  Suction  and  Discharge .': 290 

Air  Compression  at  Altitudes : 17    70,  73 

Air  Compressors 

Capacity  of ." - 18 

Circulating  Water  for - 26 

Classification  of 36 

Direct  Acting 1 -  345,  375 

Displacement  of 18 

Drives 36 

Duplex,  Belt  and  Steam 41-45 

Effect  of  Intake  Temperatures 70 

Efficiency,  Volumetric  and  Mechanical ! 14,  17,  19 

Foundations  for.. ... , 21 

Gas  or  Gasoline  Extraction 39B 

General  Construction.. 26 

Inspection  and  Cleaning  of 25 

Installation  and  Operation  of.... - 20 

Location  of 20 

Lubrication — 15,  22 

vSingle,  Belt  and  Steam 39-40 

Steam  Consumption 37 

Uses 47-51 

Valve  Gear 32 

Vertical 45-46 

Air  Compressors,  Gas  or  Gasoline  Extraction 39B 

Air  Consumption  of  Tools  and  Machines .• 87-88 

Air  and  Circulating  Pumps 213 

Air  Cylinders 32 

Air  Cylinders,  Displacement  of —. - 65 

Air  Drills ......< 78 

Air,  Flow  Through  Round  Holes 77 

Air  Inlet  Piping 21 

Air  Lift  Advantages 57 

Air  Lift  Calculations 61-62 

Air  Lift  Data  Table :. 63 

Air  Lift  Installation , 59 

Air  Lift  Piping 60 

Air  Lift  Terms 57 

Air,  Loss  of  Pressure  in  Pipes  and  Valves 80-83 

Air  Pipes,  Carrying  Capacity. —     79 

M73430 


Air  Receivers •. 22,  46 

Air,  Removing  Moisture 14 

AirValves._ .'. 30-31 

Air,  Volumes  of  Free  Air 84 

Air,  Weight  at  Various  Pressures 85 

Alternating  Current 233 

Alternating  Current  Motors 234 

Amperes 230 

Ampere  Ratings  A.  C.  Motors 238 

Ampere  Ratings  D.  C.  Motors :..*.". 239 

Areas  of  Circles 427-431 

Areas,  Ratio  of .  307-308 

Asphaltic  Base  Oils ..  24-453 

Automatic  Centrifugal  Pumps  and  Receivers,  Motor  Driven 107A 

Automatic  Feed  Pumps  and  Receivers,  Burnham 350 

Automatic  Feed  Pumps  and  Receivers,  Union  Duplex 351B 

B 

Ball  Valves 311 

Barometer,  Reduction  to  Sea  Level - 332 

Baume  Scales - 447 

Belt  Driven  Dry  Vacuum  Pumps 215,  390 

Better  Lubrication 15 

Bevel  Seat  Valves 311 

Boiler  Feed  Pumps 314 

Boiler  Feed  Pumps,  Centrifugal 106 

Boiler  Feed  Pumps,  Duplex f 350-351 

Boiler  Feed  Pumps,  Simplex 348-349 

Boiler  Feed  Pump  and  Receivers,  Centrifugal .L 107A 

Boiler  Feed  Pump  and  Receivers,  Duplex 351B 

Boiler  Feed  Pump  and  Receivers,  Simplex 350 

Boiler  Feed  Pump  Ratings,  Simplex  and  Duplex 315 

Boiling  Points  of  Liquids 331 

Boyle's  Law 3 

Brake  H.  P.  of  Air  Compressors 38 

Brass  Tubing,  Weight  of -  218-225 

Bronze  Valves 310 

Burnham  Steam  Pumps 260 

Burnham  Valve  Gear,  Directions  for  Setting 262 

C 

Cables  and  Ropes 442 

Calorific  Power  of  Fuels - 437 

Capacity  of  Air  Compressors 18 

Capacity  of  Cylinders— -  306 

Capacity  of  Pumps --  294 

Capacity  of  Pumps,  Table 305 

Cargo  Oil  Pumps,  power  driven -  393B 

Cargo  Oil  Pumps,  steam  driven : 351B 

Casing  Head  Gasoline 456 

Center  Packed  Plunger  Pumps 271,  352 

Centrifugal  Pumps 

Advantages 

Characteristics  and  Explanations ..-•. -  117-120 

II 


^T7TTTTTTrTrrg»^^ 


Centrifugal  Pumps — Continued 

Data .,..  100 

Directions  for  Installing  and  Operating    129-130 

Efficiency - 121 

Head  Determination. 1 08-109 

Horse  Power  Calculations 132 

Ifs 131 

Multi-Stage _• 107 

Power  Consumption 141 

Priming 126-127 

Pumps  and  Receivers : 107A 

Relation  of  Capacity,  Head,  Speed  and  Horse  Power 121-122 

Side  Suction  Pumps 103-104 

Sump  Pumps,  Single  and  Duplex .—  107B 

-Uses 97-99 

Centrifugal  House  Pump 107C 

Centrifugal  Pumps,  Double  Suction,  High  Speed 106 

Centrifugal  Pumps,  Double  Suction,  Horizontally  Split  Case 105 

Centrifugal  Pumps,  Multistage 107 

Centrifugal  Pumps  for  Paper  Stock 107D 

Centrifugal  Pumps  and  Receivers 107A 

Centrifugal  Pumps 90 

Characteristics  of  Average  Oils — .  476 

Characteristics  of  Tested  Oils 475 

Charles'  Law 3 

Chemical  Properties  of  Petroleum  : 451 

Choice  of  Condensers 181-182 

Circles,  Areas  and  Circumference.. ._ 427-431 

Circular  Measure  _ 441 

Circulating  Water  for  Compressors 26 

Circumference  and  Areas  of  Circles 427-431 

Clapper  Valves 311 

Classification  of  Air  Compressors 36 

Co-Efficients  of  Linear  Expansion 432 

Comparative  Economy  of  Turbines  and  Engines.— 179 

Comparative  Table  U.  S.  and  Metric  System _ 435-436 

Comparison  of  Hydrometer  Scales .-. 333-334 

Comparison  of  Thermometers 424 

Compound  Pumps,  Center  Packed 357 

Compound  Pumps,  End  Packed 358 

Compound  Pumps,  Heavy  Piston 355 

Compound  Pumps,  Light  Service 356 

Compound  Pumps,  Pot  Valve 359 

Compound  Steam  Cylinder  Calculations..... ,. 280-281 

Compound  Steam  Cylinder  Pumps 279 

Compound  Steam  Cylinder  Table 282 

Compressed  Air 

Data 52 

Multipliers  for ., 71 

Principles  of _ 2 

Table  for  Hoisting  Engines 74 

Table  for  Motors 75 

Table  for  Pumps 76 

Temperature  and  Mean  Pressure 69 

III 


Compression —  Continued 

Adiabatic    .: 4-5 

Cylinder  Ratio,  Two-Stage  Compression 16 

Efficiency 19 

Isothermal 6-7 

Loss  of  Work  Due  to  Heat 68 

Multi-Stage 12 

Single  and  Two  Stage 10,  66 

Temperature  of  Cylinders .r 23 

Three  and  Four  Stage 67 

With  Clearance 8 

Compressor  Installation  and  Operation 20 

Condensers 

Auxiliaries 186,  187,  208-215 

Cooling  Water 185-205 

Installation.... 227-228 

Jet 188-190 

Power  Saving 167-173 

Principles 166,  183-184 

Selection  of 181-182 

Surface 197-201 

Surface,  High-Vacuum  Type. 203 

Connecting  Rods 28 

Consumption  of  Electricity  for  Pumping 141 

Consumption  of  Gasoline  for  Pumping 141 

Contents  of  Cylinders- 79 

Contents  of  Cylindrical  Tanks 416 

Convenient  Equivalents 156-158 

Cooling  Water  for  Condensers 185 

Cooling  Water  for  Surface  Condensers 205 

Correct  Cylinder  Ratios,  Two  Stage  Compression 16 

Cost  of  Compressed  Air,  Electric  Driven  Compressors 55 

Cost  of  Compressed  Air,  Gasoline  Driven  Compressors 55 

Cost  of  Compressed  Air,  Steam  Driven  Compressors 54 

Cost  of  Pumping 133 

Cracking  Process  in  Oil  Refining..... 455 

Crank  and  Fly  Wheel  Pumps,  Classification ..  383 

Crankshaft 27 

Creating  a  Vacuum  in  a  Closed  Tank 404-405 

Cross  Cracking  Unit,  flow  diagram 457 

Crossheads 29 

Cubic  Feet  of  Air  for  Drills 78 

Cubic  Measure 441 

Cylinders 

Capacity  of,  Gallons 306 

Contents  of,  Cubic  Feet 79 

Piston  Displacements,  Cubic  Feet 86 

Cylinder  Temperatures— 23 

D 

Data  for  Centrifugal  Pumps 100 

Data  for  Deep  Well  Pumps 347 

Data  for  Direct  Acting  Pumps - 346 

Data  for  Power  Pumps  and  Crank  and  Fly  Wheel  Pumps 386 

Decimal  Equivalents 425 

IV 


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Decimal  Equivalents  of  Millimeters -  426 

Deep  Well  Pumps 342 

Deep  Well  Pumps  Data -  347 

Deep  Well  Pump  Table - 377 

Density  of  Gases  and  Vapors 70 

Determination  of  Total  Head  of  Centrifugals 108-109 

Diagram  of  Air  Lift— 58 

Diagrammatic  Arrangement  of  Triple  Effect  Evaporator....  324 

Diameters  of  Pulleys * : 154 

Direct  Acting  Air  Compressors 345 

Direct  Acting  Air  Compressor  Table 375 

Direct-Acting  Pumps  Data 346 

Direct  Acting  Steam  Pump  Classification 258 

Direct  Current 234 

Direct  Current  Motors 238 

Directions  for  Installing  Centrifugal  Pumps 129 

Directions  for  Operating  Centrifugal  Pumps 130 

Directions  for  Setting  the  Burnham  Valve  Gear 262 

Directions  for  Setting  Valves  of  Duplex  Pumps 266 

Discharge  Nozzles 115 

Discharge  Piping 22 

Discharge  of  Water  from  Nozzles 149 

Displacement  of  Air  Compressors 18 

Displacement  of  Air  Cylinders 65 

Displacement  of  Pumps 293 

Displacement  of  Pumps  for  Evaporator  Work '., 322 

Ditches 159 

Distillation  of  Petroleum . 454 

Double  Suction  Pumps '.... 95 

Double  Suction  Pumps,  Horizontally  Split  Case  Type 105-106 

Driei  Air 14 

Dry  Measure 441 

Dry  Vacuum  Pumps,  Duplex  Belt 394 

Dry  Vacuum  Pumps,  Duplex  Steam 402 

Dry  Vacuum  Pumps,  Single  Belt 390 

Dry  Vacuum  Pumps,  Single  Steam 399 

Duplex  Air  Compressors: 

Class  DEL  Belt 41 

Class  BD  Belt 41 

Class  DSL  Steam , : 42 

Class  SD  Steam 42 

Class  DBTL  2-Stage,  Belt . 43 

Class  BDT  2-Stage,  Belt 43 

Class  DSTL  2-Stage,  Steam.. .' 44 

Class  SDT  2-Stage,  Steam 44 

Class  CTD  Cross  Compound,  2-Stage 45 

High  Pressure  Gas  Compressors 39B 

Duplex  Boiler  Feed  or  Pressure  Pumps— 351 

Duplex  Pressure  Oil  Pumps 351A 

Duplex  Pumps,  Directions  for  Setting  Valves 266 

Duplex  Crank  and  Fly  Wheel  Dry  Vacuum  Pumps 402 

Duplex  Crank  and  Fly  Wheel  Wet  Vacuum  Pumps 401 

Duplex  Dry  Vacuum  Pumps,  Belted 394 


Duplex  Light  Service  Pumps _ 363 

Duplex  Power  Oil  Line  Pumps 393A 

Duplex  Power  Pumps 393 

Duplex  Piston  Pumps,  Horizontal 264 

Duty 300-302 

Duty  Table 303 

E 

Economy  Rating  of  Evaporators^ „ 329 

Economy  of  28"  Vacuum  over  26" .'..'. 176 

Effect  of  Intake  Temperatures 70 

Efficiency  of  Air  Compression  at  Altitudes 70 

Efficiency  of  Centrifugal  Pumps 121 

Efficiency  of  Induction  Motors 237 

Efficiency  of  Power  Pumps 384 

Elbows,  Loss  of  Pressure _ 83 

Electrical  Accessories 252-255 

Electrical  Control,  Manual  and  Automatic  for 

Air  Compressors 240-252 

Centrifugal  Pumps 240-252 

Power  Pressure  Pumps 240-252 

Power  Vacuum  Pumps :... 240-252 

Electrical  Equivalents 233 

Electrical  Units 230-232 

Electric  Gear  Driven  Pumps 382 

Elevations  of  Various  Cities 332 

Elevator  Pumps 318 

End  Packed  Plunger  Pumps 272 

End  Packed  Plunger  Pump  Table 353 

End  Packed  Pot  Valve  Plunger  Pump  Table  Simplex 354 

End  Packed  Pot  Valve  Plunger  Pump  Table  Duplex 354 

End  Packed  Pot  Valve  Pumps 273 

Engines,  Horsepower  of 417 

Engines,  Steam  Consumption 174 

Equivalents,  Table 156-158 

Evaporation 1 411 

Evaporation  in  a  Vacuum 321 

Evaporator,  Diagrammatic  Arrangement  of  Triple  Effect 324 

Evaporators,  Multiple  Effect 323 

Evaporators,  Rating  of —  329 

Evaporator  Work,  Displacement  of  Pumps 322 

F 

Factors  of  Evaporation ^ 411 

Feed  Pumps,  Ratings,  Simplex  and  Duplex 315 

Feed  Pumps  and  Receivers 316 

Feed  Pumps  and  Receivers  Table 350 

Feed  Water  Pumps -  314 

Feed  Water  Pumps,  Duplex .  350-351 

Feed  Water  Pumps,  Simplex 348-349 

Flanges -  412-413 

Flow  Diagram  Cross  Cracking  Coil 457 

Flow  of  Air  Through  Round  Holes 77 

Flow  of  Water  in  Flumes 164 

VI 


^ 


Foamite  Pump , 473 

Foundations  for  Air  Compressors 21 

Friction  of  Oil  in  Pipes,  Formula 475 

Friction  of  Oil  in  Pipes,  Table..... ...... 477-478 

Friction  of  Paper  Stocks  in  Pipes 443—446 

Friction  of  Pipe  Fittings 148 

Friction  of  Water  in  Elbows 146-147 

Friction  of  Water  in  Pipes 144-145 

Fuel,  Calorific  Power  of 437 

Full  Load  Speed  of  Induction  Motors 237 

G 

Gain  in  Compounding  Pumps 280 

Gain  in  Thermal  Efficiency 172 

Gas  or  Gasoline  Extraction  Compressors _ 39B 

Gases  and  Vapors,  Density  of 70 

Gasoline  Pumps 464 

Gear  Driven  Pumps 382 

Gears  and  Pulleys,  Rules  for  Sizes 153 

General  Construction  of  Air  Compressors 26 

Gunter'-s  Chain 442 

H 

Handling  Hot  Water 287 

Head  in  Feet  of  Water  and  Mercury  Equivalents 142-143 

Head,  Measurement  of 292 

Heating  Systems,  Steam  Required 336 

High  Vacuum  Pumps 320 

High  Vacuum  Pump  Table 368-370 

High  Vacuum  Surface  Condensers 203 

Horizontal  Duplex  Boiler  Feed  or  Pressure  Pumps 351 

Horizontal  Mine  Pumps— 365 

Horizontal  Piston  Pumps,  Duplex 269 

Horizontal  Piston  Pumps,  Simplex 267 

Horsepower  of  Centrifugal  Pumps,  Calculation. 132 

Horsepower,  Efficiency  and  Temperatures  of  Single  and  Two  Stage 

Compression. 66 

Horsepower,  Efficiency  and  Temperatures  of  Three  and  Four  Stage 

Compression. 67 

Horsepower  of  Engines 417 

Horsepower — Hour 232 

Horsepower  of  Motors '. 233 

Horsepower  of  Power  Pressure  Pumps,  Calculation  of 384-385 

Horsepower  of  Power  Vacuum  Pumps,  Calculation  of 385 

Horse  Power  Ratings,  Duplex  Boiler  Feed  Pumps.... 315 

Horse  Power  Ratings,  Simplex  Boiler  Feed  Pumps 315 

Hot  Oil  Pumps 

Forged  Steel  Compound 468 

Forged  Steel  Duplex 46  9 

Forged  Steel  Simplex 468 

Twin  Forged  Steel  Compound  Plunger  472 

Twin  Forged  Steel  Piston... 470 

Twin  Forged  Steel  Plunger 471 

Twin  Valve  Pot  „ 466^-467 

Valve  Pot  Duplex : 465 

Valve  Pot  Simplex . 465 

VII 


House  Pump,  Centrifugal 107C 

Hydrant  and  Hose  Stream  Data 150-151 

Hydraulic  Efficiency 295 

Hydraulic  Pressure  Pumps 274,  341 

Hydraulic  Pressure  Pumps,  Cast  Iron  Cylinder  Table 373 

Hydraulic  Pressure  Pumps,  Forged  Steel  Cylinder  Table 374 

Hydrometer  Scales.- 333-334 

Hyperbolic  Logarithms : 226 

I 

Impellers 91 

Impeller  Diagram 101 

Impeller  Theory.- 102 

Indicated  H.  P.  of  an  Air  Compressor 38 

Indirect  Radiation. 336 

Induction  Motors.- 234 

Information  for  Air  Lift 64 

Inspection  and  Cleaning  of  Air  Compressors 25 

Intercooler 13 

Inverted  Suction  Valve  Vacuum  Pumps 371 

Irrigation 158 

Irrigation  Table 161-162 

Isothermal  Compression 6 

J 

Jet  Condensers 188-190 

Jet  Condenser,  Calculations : 194-197 

Jet  Condenser  Installation 191 

Jet  Condensers,  Table 214 

Joule 232 

Joules'  Law 3 

K 

Kilovolt 230 

Kilovolt-Ampere 232 

Kilowatt 231 

Kilowatt-Hour 232 

L 

Land  Measure 442 

Light  Service  Horizontal  Piston  Pumps 360-361 

Light  Service  Vertical  Piston  Pumps 362 

Location  of  Compressors ; 20 

Logarithms 419-420 

Logarithms,  Hyperbolic * 226 

I/css  of  Heat.  Simple  and  Compound  Compression 68 

Loss  of  Pressure  in  Air  Pipes,  75  Ibs 80 

Loss  of  Pressure  in  Air  Pipes,  90  Ibs 81 

Loss  of  Pressure  in  Air  Pipes,  100  Ibs 82 

Loss  of  Pressure  in  Air  Valves,  Tees  and  Elbows 83 

Low  Vacuum  Pumps  __ 335 

Low  Vacuum  Pumps,  Table 366-368 

Lubrication 

Compressor  Cylinder 

Steam  Cylinder 25 

VIII 


M 

Magma  Pumps,  Belt 391 

Magma  Pumps,  Steam  344 

Magma  Pumps,  Table 378 

Materials  and  Manner  of  Fitting  Centrifugal  for  Different  Liquids..  137-140 
Materials  and  Manner  of  Fitting  Reciprocating  Pumps  for  Different 

Liquids 297-299 

Measures  of  Length 442 

Measurement  of  Power— 1 16 

Measurement  of  Speed 116 

Measurement  of  Total  Head 292 

Measurement  of  Water. 1 10 

Mechanical  Efficiency  of  Air  Compressors 17 

Mechanical  Efficiency  of  Pumps- 295 

Melting  Points ,. 432 

Mensuration  of  Surfaces  and  Volumes.- 433-434 

Metal  Compositions,  Proportion  of .... 438 

Metallic  Packing.- 313 

Methods  of  Priming  Centrifugal  Pumps 126-127 

Metric  Conversion  Table 436 

Milk  Pumps 343 

Milk  Pumps,  Table 378 

Millivolt 230 

Mine  Pumps.- 317,  364,  365 

Most  Economical  Vacuum  for  Steam  Engines 173 

Most  Economical  Vacuum  for  Steam  Turbines : 174 

Motors 

Alternating  Current 233-238 

Direct  Current 238-239 

Induction , 236 

Selection  of 240 

Slip  Ring 235 

Squirrel  Cage 235 

Multiple-Effect  Evaporators 323 

Multipliers  for  Air  Drills . 78 

Multipliers  for  Compressed  Air— 71 

Multi-Stage  Compression.- 12 

Multi-Stage  Turbine  Pumps 107 

N 

Natural  Trigonometric  Functions 42 1-423 

Nozzles  for  Water  Measurement 115 

Nozzles,  Discharge  of  in  G.  P.  M 149 

o 

Ohm's  Law 230 

Oils,  Characteristics  of 475-476 

Oils,  Viscosity  Chart 479 

Oil 

For  Air  Compressors,  Steam  Cylinder 25 

For  Air  Cylinders... 25 

Table 476 

Useful  Information 475 

IX 


Oil  Pumps 

Cargo  Loading  Pumps 474 

Centrifugal  Pumps  for  Light  Oils ,... 464 

Centrifugal  Gasoline  Pumps , 464 

Duplex  Pumps 461 

Duplex  Oil  Line  Pumps  Steam 462 

Duplex  Oil  Line  Pumps  Power , 393A 

Duplex  Plunger  High  Pressure  Pumps 463 

Foamite  Pumps 473 

Forged  Steel  Hot  Oil  Compound ---'- : 468 

Forged  Steel  Hot  Oil  Duplex .' 469 

Forged  Steel  Hot  Oil  Simplex 468 

Multi-Stage  for  Oils  and  Water 464 

Separate  Chest . 461 

Simplex  Piston ... .  461 

Simplex  Plunger  High  Pressure — - 462 

Sludge  Pumps 474 

Valve  Pot  Hot  Oil  Simplex '. 465 

Valve  Pot  Hot  Oil  Duplex..... -- - ....  465 

Valve  Pot  Hot  Oil  Twin .... -  466-467 

Twin  Forged  Steel  Hot  Oil  Piston 470 

Twin  Forged  Steel  Hot  Oil  Plunger 471 

Twin  Forged  Steel  Hot  Oil  Compound  Plunger 472 

Oils,  Characteristics  of 476 

Open  Pot  Water  Seal - 313 

Operation  of  Burnham  Pumps 261 

Operation  of  Turbines  at  High  Vacuums - 177-178 

Outside  Center  Packed  Pumps 271 

Outside  End  Packed  Pumps 272 

P 

Packing,  Metallic -..' - - 313 

Paper  Stock  Pump,  Centrifugal  Type 107D 

Paper  Stock,  Friction  in  Pipes 443-446 

Paraffin  Base  Oils - 24-453 

Performance  Factors  of  Pumps.- - - 292 

Physical  Properties  of  Petroleum 452 

Pipe,  Radiating  Surf  ace  of - - 340 

Piping,  Dimensions  and  Weights - 414-415 

Piping,  Discharge 22 

Piston  Speeds  for  Pumps - 292 

Pitot  Tube 115 

Plain  Belted  Power  Pumps 381 

Plunger  Pumps - >.  -  -  271,  272,  352-354 

Pot  Valve  Pumps,  Simplex 273,  354 

Pot  Valve  Pumps,  Duplex -  274-354 

Power  Factor 

Power  Factor  for  Induction  Motors -  237 

Power  Magma  Pumps --  391 

Power,  Measurement  of 116 

Power  Pumps,  Advantages  of  Different  Types  of  Drives  ..  382 

Power  Pump  Classification _ 

Power,  Pump  Data 386 

Power  Pumps,  Efficiency  of 384 

X 


B  ATTLE      CREEK.     MICHIGAN.      U.S.A. 

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Power  Pumps,  Single  Light  Service 388 

Power  Pumps,  Single  Pressure . 387 

Power  Pumps,  Duplex 393 

Power  Pumps,  Duplex  Oil  Line 393A 

Power  Pumps  Single  Enclosed 392 

Power  Required  for  Condenser  Auxiliaries 212-213 

Power  Saving  with  Condenser 167-173 

Pressure  Conversion  Factors 331 

Pressure  Loss  in  Air  Pipes — 80-83 

Pressures  for  Stage  Compression. 15 

Prime  Movers  for  Centrifugals 123 

Prime  Movers,  Steam  Consumption 417 

Priming  Centrifugal  Pumps 126-127 

Principles  of  Compressed  Air 2 

Principles  of  Multiple  Effect  Evaporators 323-327 

Principles  of  Surface  Condensers 183-185 

Properties  of  Saturated  Steam  for  Condensers 206-207 

Proportions  of  Various  Compositions 438 

Pulleys  and  Gears 153 

Pulleys  and  Gears,  Rules  for  Sizes 153 

Pulleys,  Diameter  of : 154 

Pumping  Cost 133 

Pumping  Liquids  Other  Than  Water. 134-136 

Pumping  With  Compressed  Air 57 

Pumps  for  the  Oil  Industry 458 

Pumps 

Advantages  of  Duplex 266 

Capacity  of 305 

Centrifugal  Pumps  and  Receivers  _ 107A 

Displacement  of 293 

Duplex  Pumps  and  Receivers 351B 

Mechanical  Efficiency 295 

Performance  Factor 292 

Piston  Speed  292 

Power 380 

Simplex  Pumps  and  Receivers 350 

Steam 258 

Table  of  Capacity 305 

Valves 309 

Volumetric  and  Mechanical  Efficiency 294-295 

Q 

Quantity  of  Lubricating  Oil  for  Air  Cylinders 25 

Quantity  of  Lubricating  Oil  for  Air  Compressor 'Steam  Cylinder's 25 

R 

Radiating  Surface  of  Pipe ? 340 

Ratio  of  Areas 307-308 

Ratio  of  Cylinders  for  Compound  Pumps 280 

Ratio  of  Submergence 59 

Receivers,  Air    __ 22,  46 

Reduction  of  Barometer  to  Sea  Level 332 

Refining  of  Oils 453 

XI 


}        UN 

I  ON 

STEAM 

PUMP 

C  OMPANY 

4 

Relative  Quantities  of  Water 152 

Ring  Packing  for  Fluid  Pistons 312 

Ropes  and  Cables 442 

Rules  for  Size  of  Pulleys  and  Gears 153 

s 

Saturated  Steam,  Table 406-409 

Saturated  Steam  at  High  Vacuum 176 

Saturated  Steam  for  Condenser  Work..... 206-207 

Selection  of  Motors „>.. 240 

Separate  Chest  Pumps ...  351A-461 

Short  Belt  Driven  Power  Pumps , 381 

Side  Suction  Volute  Pumps 103-104 

Simple  Cylinder  Pumps 278 

Simple  Cylinder  Pumps,  Calculation  of 278 

Single  Belted  Dry  Vacuum  Pumps 390 

Single  Crank  and  Fly  Wheel  Dry  Vacuum  Pumps 399 

Single  Crank  and  Fly  Wheel  Syrup  Pumps 400 

Single  Crank  and  Fly  Wheel  Wet  Vacuum  Pumps 398 

Single  Enclosed  Type  Power  Pumps — , 392 

Single  Piston  Pattern  Light  Service  Pumps 388 

Single  Piston  Pattern  Pressure  Pumps 387 

Single  Pumps. 259 

Single  Stage  BL,  Belt  Driven  Compressors 39 

Single  Stage  SL,  Steam  Driven  Compressors 39 

Single  Stage  Compression  at  Altitudes 72 

Single  Suction  Pumps 95 

Sinking  Pumps,  Vertical '. 365 

Size  of  Auxiliaries  for  Condensers.. , 186-187 

Size  of  Suction  and  Discharge  Pipes 288 

Slip  of  Induction  Motors 236 

Slip  of  Pumps.__ 294 

Slip  Ring  Motors 235 

Sludge  Pumps 474 

Specific  Gravity  of  Metals 438 

Specific  Gravity  of  Petroleum 452-476 

Specific  Heat  at  Constant  Pressure 4 

Specific  Heat  at  Constant  Volume 3 

Speed  of  Induction  Motors 236 

Speed,  Measurement  of 116 

Speed,  Pumps 292 

Squirrel  Cage  Motors 235 

Standard  Pattern  Wet  Vacuum  Power  Pumps 389 

Steam  Consumption  of  Air  Compressors.. 37 

Steam  Consumption  of  Engines 174 

Steam  Consumption  of  Prime  Movers 417 

Steam  Consumption  of  Turbines- 178 

Steam  Cylinders 33 

Steam  Cylinder  Lubrication 25 

Steam  Driven  Dry  Vacuum  Pumps - 215 

Steam  Economy  of  Pumps 304 

Steam  Indicated  Horse  Power. 296 

Steam  Pumps.- 258 

Steam  Required  by  Heating  Systems 336 

XII 


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BATTLE      C  REE  K .     M  I  CHI  G  AN ._  JLL_  _S,^V 


Steam  Table  for  Evaporator  Work 330 

Steam  Turbines -  125 

Straight  Distillation  of  Petroleum 454 

Stuffing  Boxes 

vSuctionat  Altitudes 

Suction  Air  Chambers - 291 

Suction  Denned 

Suction  Lift  Diagram  for  Centrifugal  Pumps 128 

Suction  Pipe 287 

Sump  Pumps —  107B 

superheated  Steam  Table : 410 

Surface  Condenser  Calculations -— 185 

Surface  Condenser  Construction 197 

Surface  to  Condense  Steam  Under  Different  Conditions 204 

Surface  of  Tubes  for  Condensers ~- 216 

Synchronous  Motors 234 

Syrup  Pumps,  Crank  and  Fly- Wheel- -  400 

T 

Table  of  Branch  Pipes - 79 

Table  of  Degrees,  Brix. 448 

Table  Giving  Injection  Water,  Vapor  and  Displacements  for  Jet 

Condensers 192-193 

Table  of  Horse  Power  Ratings,  Duplex  Feed  Pumps - 315 

Table  of  Horse  Power  Ratings,  Simplex  Boiler  Feed  Pumps 315 

Tanks,  Contents  of - -  -  416 

Tank  Pumps -  360-364 

Tees,  Loss  of  Pressure  in - 83 

Tests  of  Turbines..™ - 178 

Theoretical  Capacity  of  Pumps 305 

Theoretical  Horse  Power  to  Raise  Water 155 

Thermal  Efficiency 172 

Thermometers 424 

Three  Ring  Fluid  Piston  Packing 312 

Triple  Effect  Evaporator 328 

Triplex  High  Pressure  Milk  Pumps 396 

Triplex  Plunger  Pumps.- 395 

Tubes,  Surface  in  Square  Feet 217 

Turbine  Pumps 92 

Turbines,  Operation  of  at  Different  Vacuum :. 177—178 

Turbo-Generators,  Water  Rates 180 

Twin  Pumps : 459 

Two  Stage  Air  Compression 10 

Two  Stage  Compression  at  Altitudes.- 73 

Two  Stage  Single  Acting  Belt  Driven  Compressors 40 

Two  Stage  Double  Acting  Belt  Driven  Compressors 39A 

Two  Stage  Single  Acting  Steam  Driven  Compressors 40 

Two  Stage  Double  Acting  Steam  Driven  Compressors. 39A 

Types  of  Compound  Pumps 283 

Types  of  Drives  for  Air  Compressors 36 

U 

U.  S.  Standard  Flanges.- 412 

U.  S.  Standard  Flanges,  Extra  Heavy 413 

XIII 


UNION       STEAM       PUMP       COMPANY 


U.  S.  System  and  Metric  Comparative  Tables 435-436 

Useful  Data 331 

Useful  Information,  Oil 475 

Uses  of  Centrifugal  Pumps 97-99 

Uses  of  Compressed  Air 47 

Use  of  Hydraulic  Pressure  Pumps 341 


v 

Vacuum  at  Sea  Level 175 

Vacuum,  Economy  of  28"  Vacuum  Over  26" 176 

Vacuum,  Feet  Conversion  Table. . 152 

Vacuum  for  Steam  Engines 173 

Vacuum  for  Steam  Turbines 174 

Vacuum  Heating  Pumps,  Calculation  of.. 338 

Vacuum  Heating  System 337 

Vacuum  in  Closed  Tank 404-405 

Vacuum  Pans 322 

Vacuum  Pumps 

Crank  and  Flywheel,  Wet  Vacuum. 398-401 

Dry  Vacuum 390,  394,  399,  402 

High-Vacuum,  Uses 320 

Inverted  Suction- Valve 371 

Low  and  High  Classification 319-320 

Low- Vacuum,  Uses 335 

Tables,  Low  and  High 366-371 

Wet  Vacuum,  Power  Driven 389 

Wet  Vacuum,  Steam  Driven 366-372 

Valves,  Air 30-31 

Valve  Area 309 

Valve  Gear  for  Air  Compressors — .     32 

Valve  Motion,  Burnham  Pumps.— 260 

Valve  Motion  Duplex  Pumps 264 

Valves,  Pump 309-312 

Vapors  and  Gases,  Density  of 70 

Velocity  of  Flow  Through  Pipes 1 - 163 

Velocitv  of  Water  in  Ditches.. '. 160-161 

Venturi  Meter 114 

Vertical  Air  Compressors,  Single  and  Duplex 45-46 

Vertical  Boiler  Feed  or  Pressure  Pumps 349 

Vertical  Duplex  Boiler  Feed  or  Pressure  Pumps 351 

Vertical  Duplex  Light  Service  Pumps 364 

Vertical  Light  Service  Pumps 362 

Vertical  Piston  Pumps 276 

Vertical  Sinking  Pumps 365 

Vertical  Vacuum  Pumps 372 

Viscolizer 397 

Viscosity  of  Oils 452-479 

V.  Notch  Weir 114 

Voltage 230 

Volumes  of  Dry  Saturated  Steam  at  High  Vacuums 176 

XIV 


Volumes  of  Free  Air 84 

Volumes,  Mean  Pressure  and  Temperature  of  Compressed  Air 69 

Volumetric  Efficiency  of  Compressors 14-19 

Volumetric  Efficiency  of  Pumps 294 

Volute  Pumps 94 

w 

Water,  Flow  in  Flumes 164 

Water,  Flow  Through  Pipes .... 163 

Water,  Hot,  Handling  of 287 

Water  for  Irrigation : 158 

Water  Horse  Power 296 

Water,  Measurement  of — 110 

Water  Piston  and  Plunger 312 

Water  Rates  of  Turbo-Generators 180 

Water,  Relative  Quantities - 152 

Water  Seal,  Open  Pot . 313 

Water,  Velocity  in  Ditches 160-161 

Water  Works  Pumps . 316 

Weight  of  Air.... 85 

Weight  of  Brass  Tubing 218-225 

Weights  of  Materials- 439-440 

Weights  and  Specific  Gravity  of  Liquids 440 

Weights  and  Specific  Gravity  of  Metals 438 

Weir  Box...- Ill 

Weir  Table : 112-113 

Well  Pumps : 342,377 

Wet  Vacuum  Power  Pumps 389 

Wet  Vacuum  Pumps 319 

Wet  Vacuum  Pumps,  Crank  and  Fly  Wheel 398,  401 

Wire  Gauge  Standards 418 

Work  of  Adiabatic  Compression 5 

Work  of  Isothermal  Compression 7 

Work  of  Two  Stage  Compression 10 

Wrought  Iron  Pipe 414 

Wrought  Iron  Pipe,  Extra  Strong 415 

Wrought  Iron  Pipe,  Double  Extra  Strong.- 415 


XV 


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FOREWORD 

Authentic  information  on  the  proper  selection,  installation 
and  operation  of  Pumping  Machinery,  Air  Compressors  and 
Condensers,  has  long  been  the  source  of  constant  search  by 
engineers,  architects  and  those  interested  in  either  the  theory 
or  practical  application  of  this  class  of  machinery. 

Thirty  successful  years  in  the  manufacture  of  this  product 
has  brought  to  us  the  realization  of  the  need  of  a  practical  and 
condensed  collection  of  this  data,  and  we  have,  for  the  con- 
venience of  our  friends,  compiled  this  Union  Engineering 
Handbook  devoted  to  the  theory  and  practice  in  design  and 
use  of  Air  Compressors,  Centrifugal  Pumps,  Condensers,  Steam 
and  Power  Pumps. 

This  book  is  presented  as  typical  of  the  engineering  service 
extended  by — 

UNION  STEAM  PUMP  COMPANY, 

Battle  Creek,  Michigan. 


PUMPING    MACHiNfiRY,  lAIR_^QMPRESS  QRS  __ 

~*4mm*k™»w*w»^^r*r^-?fW^^vrirf-ir^v  if vi  wvivw &•«•«  "»'a  »  nrwwwwvm  ait  a  am  gYTg-g-nzwur  »»»*»»  t  a  1  BW^Ja 


* 


Air 
Compressors 


SECTION  ONE 

fe 

b 

2^~ "  ___ 


a 


UNION       STEAM       PUMP       COMPANY 


Compressed  Air  and  Air  Compressors 

Scarcely  an  industry  exists  that  does  not  utilize  compressed 
air  in  some  manner.  Second  only  to  electricity  in  the  extent 
and  diversity  of  application,  compressed  air  is  one  of  the  most 
important  factors  in  every  phase  in  the  art  of  manufacture.  The 
rapid  development  of  compressed  air  appliances  has  brought 
about  economical  results  that  are  reflected  in  every  field  of  indus- 
try. As  the  economical  application  of  compressed  air  is  wholly 
dependent  upon  its  economical  production,  it  is  apparent  that 
the  modern  air  compressor  must  embody  every  refinement  in 
design  and  construction. 

The  cost  of  producing  compressed  air  involves  three  separate 
items:  first,  interest  and  depreciation  on  the  amount  invested 
in  compressed  >air  equipment;  second,  operating  cost;  third, 
maintenance  or  upkeep  cost.  To  minimize  the  cost  of  production, 
it  is  necessary  to  minimize  each  and  every  one  of  the  above  items. 

As  all  three  items  depend  upon  the  design  and  construction 
of  the  air  compressor,  good  judgment  and  experience  recommend 
as  the  best  investment  the  purchase  of  a  strictly  high  grade 
compressor,  commanding  a  fair  price  which  is  a  true  measure  of 
its  value  and  which  covers  a  construction  insuring  the  lowest  oper- 
ating and  upkeep  cost.  In  Union  Air  Compressors  will  be  found 
these  necessary  requirements. 

The  selection  of  the  type  of  compressor  depends  entirely 
upon  local  conditions.  Where  steam  is  available,  a  steam  driven 
unit  is  most  desired.  The  steam  cylinder  constitutes  a  very 
efficient  steam  engine,  and  the  power  is  transmitted  direct, 
eliminating  transmission  losses  and  saving  the  expense  of  belts, 
shafts,  pulleys,  etc.  On  the  other  hand,  there  are  numerous 
cases  where  a  belt  driven  machine  is  far  cheaper  to  operate,  and 
the  purchaser  is  always  best  competent  to  judge  which  type  is 
the  more  desirable. 

Principles  of  Compressed  Air 

In  order  to  obtain  an  idea  of  the  subject  of  air  compression, 
there  are  certain  underlying  principles  and  laws  that  should  be 
reviewed.  On  the  following  pages  are  given  the  basic  laws  and 
formulae  for  air  compression  that  must  be  recognized  when 
studying  this  subject. 


Boyle's  Law:  At  constant  temperature,  the  volume  of 
a  gas  is  proportional  to  the  absolute  pressure  or  PV  =  P1V1 
in  which 

P  =  Initial  absolute  pressure  in  pounds  per  square  inch. 

V.  =  Initial  volume  in  cubic  feet. 

PI=  Final  absolute  pressure  in  pounds  per  square  inch. 

V\  =  Final  volume  in  cubic  feet. 

This  law  expresses  the  fact  that  if  the  pressure  on  a  certain 
volume  of  gas  is  doubled,  the  volume  will  be  one-half  the 
original  volume  (if  the  temperature  is  constant)  ,  or  conversely, 
if  at  constant  temperature,  the  pressure  is  reduced  one-half, 
the  volume  will  be  doubled. 

Charles'  Law:  At  constant  volume,  the  pressure  of  a 
perfect  gas  is  directly  proportional  to  the  absolute  temperature 
or  at  constant  pressure  the  volume  is  directly  proportional  to 
the  absolute  temperature  or: 


T     T!  T      T! 

in  which  T  and  T:  are  initial  and  final  absolute  temperatures  in 
degrees  Fah. 

Combining  Charles'  and  Boyle's  laws,  we  have  the  tormula 
P  V_Pj  Vl 
"IT         T! 

Joules'  Law:  When  a  perfect  gas  expands  doing  no  ex- 
ternal work,  the  temperature  remains  constant.  For  example 
in  the  equation 

P  VP    V 


If  T^TiWe  have  P  V  =  Pl  Vlt  which  is  the  law  of  expan- 
sion of  a  perfect  gas. 

Specific  Heat  —  The  Specific  heat  of  a  substance  is  the 
amount  of  heat  (B.  T.  U.)  that  is  required  to  raise  the  temper- 
ature of  a  pound  of  the  substance  through  1°  Fah. 

Specific  Heat  at  Constant  Volume  Cv 

PV     PI  Vi 

In  the  equation  -  =  —  * 
T          Tj 

P      P 

If  V  =  Vithen  we  have  —  =  — 

T      T! 

which  is  the  law  of  Charles.     Suppose  we  have  a  certain  volume 


!|   '    AND 

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3 

of  air  contained  in  a  closed  receptacle,  and  the  temperature  is 
raised  1°  Fah.  The  pressure  is  thereby  raised  according  to 
the  above  law,  and  the  intrinsic  energy  of  the  air  increased. 
No  work  is  done,  however,  because  work  equals  pressure  multi- 
plied by  distance,  and  by  our  supposition  the  latter  factor  is 
zero.  At  constant  volume,  then,  the  specific  heat  of  air  is  the 
amount  of  heat  (B.  T.  U.)  that  is  required  to  raise  the  temper- 
ature of  one  pound  of  the  air  through  1  °  Fah.,  the  volume  being 
kept  constant  as  above.  Cv  for  air  is  found  by  experiment 
to  be  .1685. 

Specific  Heat  at  Constant  Pressure  CP 

Assume  in  this  instance  that  we  have  a  vertical  cylinder 
containing  a  quantity  of  air,  and  resting  on  the  air  is  a  frictionless 
piston  of  constant  weight,  or  pressure  P.  If  the  air  is  heated, 
the  volume  will  increase,  moving  the  piston  outward,  and 
external  work  is  performed.  At  constant  pressure,  then,  the 
specific  heat  of  air  is  the  amount  of  heat  (B.  T.  U.)  that  is 
required  to  raise  the  temperature  of  one  pound  of  the  air  through 
1°  Fah.,  if  the  air  is  allowed  to  expand  against  a  constant 
pressure.  Therefore  Cp  =  C  +  the  heat  equivalent  of  external 
work,  and  for  air  has  been  found  to  be  .2375.  Cp  and  Cv  are 
measured  in  B.  T.  U's.,  so  as  to  obtain  their  equivalent  in  foot 
pounds,  it  is  necessary  to  multiply  by  778,  and  the  products 
for  convenience  of  calculation  are  called  Kp  and  Kv. 

Getting  back  to  our  assumption  of  the  cylinder  and  piston 
and  assuming  further  that  we  have  (W)  pounds  of  air;  in  order 
that  external  work  be  done,  and  the  temperature  raised  1° 
Fah.,  it  is  necessary  that  W  (Cp — Cv)  thermal  units  of  heat  be 
applied,  or  W  (Kp — Kv)  foot  pounds  of  work.  In  order  to 
raise  the  temperature  T  degrees,  W  (Kp — Kv)  T  foot  pounds 
of  work  must  be  done  on  the  air.  Since  work  is  equal  to  pressure 
through  volume,  we  have 

Work  =  P  V  =  W  X  (Kp— Kv)   X  T° 
or  assuming  (Kp — Kv)  =  R,  we  have  the  formula  : 

P  V  =  W  R  T.  (1) 

Theoretically  air  may  be  compressed  in  two  ways: — 
Adiabatically  or  Isothermally. 

Adiabatic  Compression 

Adiabatic  compression  of  air  is  compression  without 
loss  of  heat.  Consider  for  example  a  perfectly  insulated  air 


cylinder  and  piston  having  full  charge  of  air  between  the  piston 
and  cylinder  head.  As  the  piston  moves,  the  volume  of  air 
becomes  smaller,  and  the  temperature  rises,  the  former  in 
inverse  proportion  to  the  absolute  pressure  exerted,  and  the 
latter  equivalent  to  the  amount  of  work  done.  Under  these 
conditions  the  air  at  the  end  of  the  compression  will  retain  all 
of  the  heat  so  produced,  and  this  particular  compression  is 
called  adiabatic.-  In  actual  practice  such  conditions  of  com- 
pression are  impossible. 

P       Vi 
In  adiabatic  compression  the  law  —  =  — 1  is  not  followed 

strictly,  because  as  the  temperature  rises  unchecked,  it  reacts 
on  the  air  being  compressed  to  increase  the  volume.  Therefore 
to  write  an  expression  for  adiabatic  compression,  it  is  necessary 

T7 

that — —be  increased  by  an  amount  equivalent  to  the  amount 

of  external  work  done  on  the  air  by  heat  reaction  during  com- 
pression. It  has  been  shown  by  various  authorities  on  heat 
or  thermodynamics  that 

P       (Vj)0.  Cp     .2375 

_=_mwluchn=^  — =1.41 

for  air  holds  nearly  tiue. 


Work  of  Adiabatic  Compression 

Figure  1  shows  the  theoretical  indicator  card  oi  an  air 
cylinder  having  no  clearance.  The  total  work  done  is  equal 
to  the  work  of  compression  shown  by  the  area  under  the  curve 
B  C,  plus  the  work  of  expulsion  of  the  air  from  the  cylinder 
shown  by  the  area  P2  V2,  minus  the  work  done  on  the  piston 
by  the  inlet  air  shown  by  the  area  Pl  Vj.  Then  calling  Q  the 
total  amount  of  work 


=  498.7  Pv--l  (2) 


and  the  horse   power  required  to  compress  1  cubic  foot  of  free 
air  per  minute  adiabatically  is 


AND    CONDENSERS    FOR    EVERY"  SERVICE 


ni^^ 


UNION       STEAM       PU  M  P       COM  P  ANY 


(3) 


Figl 

EXAMPLE:  What  horse  power  will  be  required  to  com- 
press adiabatically  1  cubic  foot  of  free  air  at  sea  level  to  100 
pounds  gauge  pressure? 

SOLUTION:  Inserting  the  above  values  in  equation  3: 


H.  P.    = 


4.5 
=  .18 


(1.81—1) 


Isothermal  Compression 

Isothermal  compression  is  compression  at  constant  tem- 
perature. In  other  words  this  is  compression  wherein  all  heat 
is  removed  by  some  form  of  cooling  device  as  fast  as  it  is  pro- 
duced. The  relation  then  existing  between  pressure  and  volume 
at  any  instant  is  shown  by  the  equation : 


PI  V,=P2  VS-C 


(4) 


E 

PUMPING 

MACHINERY, 

AIR 

COMPRESSO  R  jj["L| 

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Pig.  2. 


Work  of  Isothermal  Compression 

Fig.  2  is  the  theoretical  indicator  card  of  isothermal  com- 
pression in  a  cylinder  having  no  clearance.  The  compression 
begins  as  before  at  absolute  pressure  PI  and  volume  V\,  and 
ends  at  P2  and  V2.  The  total  work  Q  in  foot  pounds  done  on 
the  air  is  equal  to  the  algebraic  sum  of  the  work  of  the  com- 
pression, expulsion  and  the  work  done  by  the  intake  air,  and 
is  shown  in  the  following  equation : 

=  144?^  Log,  '  "• 


m 


and  the  horse  power  required  to  compress  1  cubic  foot  of  free 
air  per  minute  isothermally  is 

(6) 
Log, 


H.  P.=. 


15.6 


m 


EXAMPLE:  What  horse  power  will  be  required  to  com- 
press isothermally  1  cubic  foot  of  free  air  at  sea  level  to  100 
pounds  gauge  pressure? 

SOLUTION  :    Inserting  i,he  above  values  in  equation  6, 

r-  —i 


H.  P.  = 


15.6 


15.6 
1 

15.6 
.132 


Loge7.8 


x2.05 


AND    CONDENSERS    FOR   EVERV  SERVICE 


Actual  Compression  with  Clearance 

In  the  actual  practice  of  air  compression,  neither  of  the 
above  formulae  would  apply,  for  it  is  impossible  to  design  an 
air  compressor  cylinder  in  which  either  adiabatic  or  isothermal 
compression  can  be  obtained.  The  air  cylinder  in  practice 
is  equipped  with  a  water  jacket  for  the  remqval  of  some  of  the 
heat  <Sf  the  compression,  and  to  facilitate  lubrication,  but  all 
of  the  heat  cannot  be  removed.  A  certain  amount  is  retained 
in  the  air  itself,  and  some  is  left  in  the  cylinder  walls  and  piston. 
The  actual  compression  curve  then  will  lie  somewhere  between 
the  isothermal  and  adiabatic  curves,  and  the  exact  location 
depends  upon  the  efficiency  of  the  water  jacket,  the  temper- 
ature of  the  circulating  water,  etc. 

Also  in  the  actual  cylinder  there  is  a  certain  amount  or 
lost  space  or  clearance  in  the  ends  of  the  cylinder  between  the 
piston  and  the  heads,  and  around  the  valves,  all  of  which  has 
its  effect  on  the  shape  of  the  indicator  card.  This  clearance 
at  the  end  of  the  piston  is  filled  with  air  at  the  discharge  pres- 
sure and  temperature.  As  the  piston  recedes,  the  clearance  air 
expands,  doing  work  on  the  piston,  and  finally  the  re-expanded 
air  occupies  part  of  the  volume  of  the  cylinder  behind  the  piston. 
No  air  can  be  drawn  into  the  air  cylinder  until  the  pressure  in- 
side falls  below  that  of  the  atmosphere. 

In  the  compression  of  a  perfect  gas  receiving  heat  in  some 


Fig.  3 


I         PUMPING   MACHINERY,    A 

IR   COMPRESSORS      _| 

regular  way,  the  following  relation  of  volume  and  pressure  at 
any  instant  generally  holds  true  : 

PVn  =  C  (7) 

The  value  of  n  on  tne  ordinary  single  stage  air  compressor 
as  given  by  Church  is  1.33,  and  Unwin  as  1.25.  The  exact 
value  varies  with  the  compressor,  and  depends  upon  the  size  of 
the  cylinder,  speed  of  the  machine,  design  of  the  water  jacket, 
and  temperature  of  the  cooling  water. 

In  figure  3  is  shown  an  air  diagram  taken  from  the  cylinder 
with  clearance,  and  the  compression  curve  lies  between  the 
isothermal  and  adiabatic  curves.  The  total  amount  of  work 
done  during  the  forward  stroke  is  shown  by  the  area  A  B  C  G 
(q)  ,  but  by  the  re-expansion  of  clearance  air  there  is  an  amount 
of  work  Q1  returned  to  the  receding  piston,  shown  by  the  area 
A  F  G.  Therefore  the  net  amount  of  work  done  by  the  piston 
is  shown  by  the  area  A  B  C  F  or  Q,  and  its  value  is  given  in 
the  expression 


(V\  —  V3)  is  the  net  amount  of  air  drawn  into  the  cylinder. 
The  horse  power  required  to  compress  one  cubic  foot  of  free  air 
per  minute  is  shown  by  the  following  equation: 


.. 

15.6   (n-1)  \      14.7  / 

EXAMPLE  :    What  horse  power  will  be  required  to  actually 
compress  one  cubic  foot  of  free  air  at  sea  level  to  100  pounds 


gauge  pressure  ? 


SOLUTION:    Inserting  these  values  in  equation^. 


1.25      /ni4.7l  \ 

H.P  =  ---  (     -     J'25     -1    ) 

15.6X.25\L    14-7J  / 


=      .320     (7.8-2—  1) 
=      .320     (1.51  —  1) 
H.  P.  =      .163 


co  NE>  E N    ERS 


UN  I  O  N       S  TEAM       PU  M  P       COM  P  ANY 


Fig.  4. 

Figure  4  shows  the  actual  air  indicator  card  taken  from  a 
single  stage  air  compressor  having  disc  valves  on  the  inlet  and 
discharge.  The  areas  A  and  B  represent  the  amount  of  work 
necessary  to  open  the  discharge  and  the  inlet  valves,  and  G 
F  is  the  volume  occupied  by  the  re-expanded  clearance  air.  The 
volume  lying  between  the  suction  line  and  the  atmospheric 
line  is  the  energy  expended  to  fill  the  cylinder  with  air. 

Two  Stage  Air  Compression 

It  is  evident  now  that  isothermal  compression  requires 
the  expenditure  of  the  least  amount  of  power.  As  before 
shown  this  form  of  compression  is  impossible  in  practice,  but 
an  approach  to  it  is  realized  by  compression  in  stages,  and 
cooling  the  air  between  each  stage.  In  this  way  isothermal 
compression  is  partially  realized  as  will  be  seen  later. 

In  two  stage  compression  the  air  is  drawn  from  the  atmos- 
phere into  the  first  or  low  pressure  cylinder,  and  there  com- 
pressed up  to  a  certain  pressure.  It  is  then  discharged  through 
an  intercooler  where  the  temperature  is  reduced  by  circulating 
water,  and  then  drawn  into  the  second  or  high  pressure  cylinder 
where  the  compression  is  continued  up  to  the  desired  terminal 
pressure. 

Work  of  Two  Stage  Air  Compression 

In  a  two  stage  compressor  it  is  customary  to  proportion 
the  cylinders  so  that  the  work  is  equally  divided  between  the 
two. 

In  the  following  it  is  assumed  that  the  work  is  the  same 
in  each  cylinder,  and  further  that  the  temperature  of  the  air 


10 


CREEK.     MICHIGAN,      U.S.A. 


Fig.  5 


after  passing  through  the  intercooler  is  the  same  as  the  atmos- 
phere. 

Figure  5  shows  the  cycle  of  operation  in  a  two  stage  com- 
pressor. A  volume  Vl  of  air  under  pressure  P^  is  drawn  into 
the  low  pressure  cylinder,  and  there  compressed  to  volume  V2, 
and  pressure  P2.  The  air  is  cooled  and  the  volume  is  reduced 
to  that  shown  by  GC,  which  is  equivalent  to  the  volume  obtained 
in  isothermal  compression  from  P1  to  P2.  The  high  pressure 
cylinder  then  receives  the  air  and  compresses  it  up  to  the  pres- 
sure P4  and  volume  V4.  The  curve  of  compression  follows 
the  broken  line  EDCB. 

If  the  air  was  compressed  in  a  single  stage  compressor 
from  Px  to  P4,  the  curve  of  compression  would  be  E  I  (P  Vn  = 
C)  and  the  work  done  shown  by  area  AIEF.  The  work  done  by 
two  stage  compression  is  shown  by  the  area  ABCDEF,  and 
the  saving  realized  by  staging  is  shown  by  the  area  BIDC. 

If  Q1  and  Q2  equal  work  done  in  j:oot  pounds,  to  com- 
press air  in  the  low  pressure  and  high  pressure  cylinders  re- 
spectively, and  Q=  total  work  of  compression,  the  value  of 
Q  then  is 


n-i 


(10) 


AND    CONDENSERS    FOR   EVERY  SERVICE 


11 


The  horse  power  required  to  compress  one  cubic  foot  of 
free  air  per  minute  in  this  way,  remembering  that  (Vj_  -  V3)  is 
the  net  amount  of  air  drawn  into  the  low  pressure  cylinder,  is 


7.  8  (n-1)  \l4.7 

P2  in  equation  11  is  the  intercooler  pressure,  while  in  for- 
mulae for  work  in  single-stage  compression,  'P2  designates  termi- 
nal pressure. 

Example:  What  horse  power  will  be  required  to  actually 
compress  one  cubic  foot  of  free  air  at  sea  level,  by  two  stage 
compression,  to  100  pounds  gauge  pressure? 

Solution:  With  two  stage  compression,  P2  for  100  pounds 
pressure  is  (from  table  page  16)  26.3  -f  14.7  =41.0  pounds. 

Inserting  the  values  in  equation  11: 

1.25  -1'25-1 

H.  P.  = 


7.8     (1.25     — 

.64    (2.78-2—  1) 
.64  X   .227 
.145 

Multi-Stage  Compression  and  Its  Advantages 

Theoretically  there  is  a  gain  in  multi-stage  compression, 
whatever  the  pressure.  However,  with  low  pressures,  the  sav- 
ing is  so  small  as  to  be  offset  by  the  additional  expense  involved, 
and  the  unavoidable  mechanical  losses  in  the  operation  of  the 
additional  mechanism.  Experience  has  fixed  from  80  pounds 
to  100  pounds  gauge  as  maximum  terminal  pressures,  which 
can  be  best  attained  with  a  single  stage  compressor;  and  for 
pressures  from  80  pounds  up,  multi-stage  compression  in  two, 
three  and  four-stage  compressors  is  employed. 

In  multi-stage  air  compressors  correctly  designed,  the 
cylinder  ratios  are  such  that  the  final  temperatures,  and  mean 
effective  pressures  are  equal  in  all  cylinders,  and  all  pistons 
are,  therefore,  equally  loaded.  The  air  compressed  in  the  first 
cylinder  with  a  pressure  determined  by  the  cylinder  ratio,  is 
discharged  through  the  discharge  valves  to  an  intercooler  where 
it  is  split  up  into  thin  streams  passing  over  cold  surfaces.  Mod- 
ern practice  involves  a  nest  of  tubes  through  which  cold  water 
circulates,  and  over  and  between  which  the  stream  of  air  passes, 
complete  breaking-up  and  subdivision  of  the  stream  being  se- 


12 


P      BATTL 

E 

C 

RE 

E 

K. 

MIC 

HI 

CAN, 

U. 

S. 

A.        [ 

cured  by  baffle  plates,  and  the  tubes  themselves  (see  figure  6). 
A  properly  designed  intercooler  having  sufficient  cooling  area 
for  the  volume  of  air  may  reduce  the  temperature  of  air  com- 
pressed in  the  first  cylinder  to  at  least  the  temperature  of  the 
outgoing  water. 

Intercooler 


Fig  6. 

From  the  intercooler,  this  air,  entering  the  second  or  high 
pressure  cylinder,  is  compressed  to  a  higher  pressure,  and  again 
reaches  a  temperature  about  the  same  as  that  attained  in  the 
first  cylinder.  In  two  stage  machines,  this  air  will  be  discharged 
directly  to  the  receiver  without  further  cooling  unless  conditions 
are  such  as  to  render  necessary  the  use  of  an  aftercooler. 

The  principal  advantages  of  multi-stage  compression  are: 

Reduced  power,  higher  volumetric  efficiency,  drier  air,  and 
better  lubrication.  These  will  be  considered  in  order. 

Reduced  Power:  The  table  on  page  68  gives  the  percent- 
age of  work  lost  in  the  heat  of  compression  in  one,  two,  or  three 
stages  at  various  pressures.  In  these  figures  no  account  is  taken 
of  jacket  cooling,  nor  is  any  allowance  made  for  certain  inevitable 
mechanical  losses. 

Taking  a  specific  example,  the  saving  by  multi-staging  is 
evident.  Assuming  a  volume  of  compressed  air  equivalent  to 
100  effective  horse  power  is  to  be  delivered  at  a  pressure  of  100 
pounds. 

Referring  to  the  table  in  column  2,  the  theoretical  per- 
centage of  lost  work  in  one  stage  compression  is  given  at  36.7; 
but  because  there  is  bound  to  be  some  radiation  of  heat,  the 
value  of  36.7%  will  not  be  found  in  practice,  and  30%  may  be 
assumed  as  a  practical  figure  under  average  conditions.  On 
this  basis,  it  is  found  that  to  deliver  100  horse  power  in  com- 
pressed air  at  100  pounds  pressure,  by  one  stage  compression , 
there  will  be  required  130  indicated  horse  power.  Looking 


AND    CONDENSERS    FOR   EVERT  SERVICE 


13 


now  at  column  4  of  the  table,  the  percentage  of  loss  in  two  stage 
compression  at  this  pressure  is  found  to  be  16.9  per  cent,  which 
is  very  close  to  the  figure  found  in  practice.  Applying  this 
value,  it  is  seen  that  to  deliver  the  equivalent  of  100  effective 
horse  power  in  air  at  100  pounds  pressure,  by  two  stage  com- 
pression, about  117  indicated  horse  power  will  be  required.  In 
this  case  as  between  single  and  two  stage-compression,  we  have 
a  direct  saving  of  13  indicated  horse  power  or  10%. 

Higher  Volumetric  Efficiency:  Before  free  air  can  enter 
through  the  suction  valves,  the  air  remaining  in  the  clearance 
space  between  piston  and  head,  at  the  end  of  the  stroke,  must  be 
expanded  on  the  return  stroke  to  atmospheric  pressure.  Evidently 
the  higher  the  pressure  in  this  clearance  space,  the  greater  this 
expanded  volume,  and  the  lower  the  intake  efficiency  of  the 
cylinder.  In  single  stage  compression,  clearance  pressure  is 
the  working  pressure.  In  compound  compression,  clearance 
pressure  in  each  cylinder  is  terminal  pressure  in  that  cylinder, 
but  this  terminal  pressure  in  the  intake  cylinder  is  low,  gener- 
ally not  over  25  pounds,  when  the  final  working  pressure  is  100 
pounds.  The  volumetric  efficiency  of  a  multi-stage  compressor 
is  higher  for  this  reason,  the  clearance  -in  the  low  pressure  cylinder 
only,  being  in  question. 

Another  reason  for  higher  volumetric  efficiency  resulting 
from  multi-stage  compression  is  the  fact  that  terminal  press- 
ures, and  consequently  terminal  temperatures  are  lower  than  in 
single  stage  cylinders.  The  cylinder  walls  and  more  particular- 
ly the  heads  with  the  valves  and  ports  which  may  be  in  them 
are  therefore  kept  much  cooler,  and  the  entering  air  is  not 
much  heated  by  contact  with  these  parts.  A  third  element 
entering  into  the  question  of  capacity  is  the  reduced  leakage  in 
stage-compression  cylinders  through  valves  and  past  pistons  and 
rods  with  the  resultant  loss  of  power.  It  is  evident  that  the 
higher  the  pressure,  the  greater  liability  to  leaking;  and  the 
smaller  range  of  partly  balanced  pressures  in  multi-stage  cylinders 
reduce  this  loss. 

Drier  Air :  One  of  the  greatest  difficulties  encountered  in 
air  power  transmission  has  been  the  freezing  of  the  moisture  in 
the  air,  either  in  the  pipe  line,  or  at  the  exhaust  ports  of  the  air 
motors.  One  of  the  great  advantages  of  multi-stage  compres- 
sion lies  in  the  opportunity  it  affords  for  cooling  the  compressed 
air  between  stages  to  a  temperature  at  which  its  moisture  will 
be  precipitated.  Practically  all  of  this  condensation  occurs  in 
the  intercooler;  and  herein  appears  the  necessity  for  a  design, 


»t[ntttntt^AtKAtti.»mtttuMmK^KKminRaKnKaAKAnK^K^A^^f:^^^^^M1^SJIi^^^^A^ny\ 


14 


|       BATTLE      C 

REE 

K. 

MIC 

HIGAN, 

U. 

S. 

A. 

| 

which  will  allow  the  air  to  pass  over  the  tubes  at  a  low  velocity 
with  a  full  opportunity  for  cooling  on  the  tubes.  The  moisture 
in  suspension  is  withdrawn  through  the  drain  pipe,  which  is 
provided  at  the  lowest  point  of  the  intercooler.  Unless  the 
moisture  is  not  withdrawn  from  the  intercooler,  the  value 
of  the  latter  as  an  air  drier  is  lost;  for  the  moisture  is  carried 
over  into  the  high  pressure  cylinder,  producing  a  condition  of 
cutting  and  leakage  in  the  valves  and  rings,  and  finally  working 
into  the  pipe  line.  Aftercoolers  are  in  some  instances  as  im- 
portant as  intercoolers  in  removing  the  moisture. 

Better  Lubrication :  If  air  be  compressed  in  a  single  cylinder, 
from  atmosphere,  and  a  temperature  of  60  °  Fah.  to  a  final  pressure 
of  100  pounds,  the  maximum  temperature  will  be  484°  Fah. 
This  temperature  is  manifestly  destructive  to  common  lubri- 
cants, and  ordinary  oils  are  burned  into  a  solid  gritty  coke-like 
substance,  which  gives  the  very  reverse  to  proper  lubrication, 
unless  proper  cooling  devices  are  employed  to  keep  the  parts 
cold.  This  carbon  deposit  collecting  in  ports  and  valves  may 
so  obstruct  and  clog  them  as  to  cause  leakage  and  throw  an 
additional  load  on  the  compressor.  If,  however,  the  same 
volume  of  air  be  compressed  in  the  low  pressure  cylinder  to  a 
pressure  of  25  pounds,  the  highest  temperature  which  can  be 
reached  is  only  233°.,  a  heat  which  will  not  leave  a  deposit  or 
destroy  the  lubricating  qualities  of  good  oils  such  as  should  be 
used  in  air  compressor  work.  This  air  passing  through  the  inter- 
cooler will  be  brought  back  to  approximately  the  original  temper- 
ature of  60°,  and  compressed  in  the  second  stage,  or  high  pres- 
sure cylinder,  from  25  pounds  to  100  pounds.  Here  the  max- 
imum temperature  will  be  little,  if  any  in  excess  of  that  in  the 
first  stage  cylinder,  since  the  heat  of  compression  is  a  function 
of  the  number  of  compressions,  and  is  almost  wholly  independent 
of  initial  pressure.  In  multi-stage  compressors,  therefore,  the 
conditions  of  temperatures  are  seen  to  be  most  conducive  to 
thorough  lubrication  of  the  pistons  and  valves  tending  towards 
durability  and  tightness  of  the  working  parts  with  sustained 
efficiency  of  the  machine. 

Pressures  for  Stage  Compression 

Single  stage  compression  is  used  for  pressures  up  to  100 
pounds.  Two  stage  compression  for  pressures  from  80  pounds 
to  500  pounds,  three  stage  compression  for  pressures  500  pounds 
to  1500  pounds,  and  four  stage  compression  for  pressures  above 
1500  pounds. 


^PBg£S^.gff:?.%^.^£££J^g^g^ER'VICE" 

15 


UNION       STEAM       PUMP       COMPANV 


Correct  Cylinder  Ratios  for  Two  Stage 
Compression. 

The  correct  ratio  of  cylinders  is  obtained  by  the  following 
formula : 


or  2  stage  compression, 


(12) 


In  which  r  =  ratio  of  cylinders. 

P3  =  Absolute   terminal    pressure   in   pounds   per 

square  inch. 
P  =  Atmospheric  pressure   in  pounds  per   square 

inch. 

Thus  in  two  stage  compression,  we  extract  the  square  root 
of  the  number  of  atmospheres  to  be  compressed.  This  pro- 
portion of  cylinder  volumes  divides  the  work  equally  between 
the  different  stages. 

The  intercooler  pressure  (Pj)  in  a  two  stage  compressor 
is  obtained  by  the  following  formula : 


(13) 


In  which  Pl  =  Intercooler  pressure  oetween  first  and 
second  stages. 

The  following  table  gives  the  correct  cylinder  ratio  and 
intercooler  pressure  in  two  stage  compression  for  gauge  pres- 
sures from  50  to  500  pounds  per  square  inch. 


_o 

o 

8 

B 

*o  J3 

<3  S3 

JH 

•ss 

*-*j 

o3 

all 

||| 

H 

ill 

lai 

hr  U3  r" 

§§"•8 

11 

-4J    C    W 

8^§ 

i&l 

§  S  0 

J  1  0 

fcuJH 

•S  sl 

!|| 

log 

ll 

go| 

-11 

o£d< 

<£* 

i< 

c3-3> 

£o£ 

«££ 

cS-o> 

^oi 

50 

64.7 

4.40 

2.10 

16.2 

200 

214.7 

14.60 

3.82 

41.4 

60 

74.7 

5.08 

2.25 

18.4 

210 

224.7 

15.28 

3.91 

42.8 

70 

84.7 

5.76 

2.40 

20.6 

220 

234.7 

15.96 

3.99 

44.0 

80 

94.7 

6.44 

2.54 

22.7 

230 

244.7 

16.64 

4.08 

45.3 

90 

104.7 

7.12 

2.67 

24.5 

240 

254.7 

17.32 

4.17 

46.6 

100 

114.7 

7.80 

2.79 

26.3 

250 

264.7 

18.00 

.24 

47.6 

110 

124.7 

8.48 

2.91 

28.1 

260 

274.7 

18.68 

.32 

48.8 

120 

134.7 

9.16 

3.03 

29.8 

270 

284.7 

19.36 

.40 

50.0 

130 

144.7 

9.84 

3.14 

31.5 

280 

294.7 

20.04 

.48 

51.1 

140 

154.7 

10.52 

3.24 

32.9 

290 

304.7 

20.72 

.55 

52.2 

150 

164.7 

11.20 

3.35 

34.5 

300 

314.7 

21.40 

.63 

534 

160 

174.7 

11.88 

3.45 

36.1 

350 

364.7 

24.80 

.98 

58.5 

170 

184.7 

12.56 

3.54 

37.3 

400 

414.7 

28.20 

5.31 

63.3 

180 

194  7 

13  24 

3.64 

38.8 

450 

464.7 

31.60 

5.61 

67.8 

190 

204.7 

13.92 

3.73 

40.1 

500 

514.1 

35.01 

5.91 

72.1 

PUMPING  MACHINERY;  AIR  COMPRESSORS 


16 


i 


Air  Compression  at  Altitudes 

If  a  compressor  is  operated  at  a  greater  altitude  than  sea 
level  (14.7  pounds  per  square  inch),  the  intake  air  pressure 
will  be  proportionately  less,  and  additional  work  is  imposed 
upon  the  compressor. 

The  capacity  of  "a  given  compressor  is  less  at  higher  altitudes 
than  at  sea  level,  because  of  the  diminished  density  of  the  intake 
air. 

Volumetric  efficiency  is  also  less  at  altitudes,  due  to  the 
fact  that  the  clearance  air  expands  to  the  atmospheric  pressure 
and  consequently  when  expanding  occupies  a  larger  volume 
of  the  cylinder. 

The  table  on  page  70  gives  the  multipliers  for  compression 
at  altitudes. 

Mechanical  Efficiency 

The  mechanical  efficiency  of  a  steam  driven  compressor 
is  equal  to  the  air  indicated  horse  power  divided  by  the 
steam  indicated  horse  power  or 

_  Air  Indicated  H.  P. 
m~      Steam  I.  H.  P. 

and  the  mechanical  efficiency  of  a  power  driven  air  compressor  is 

_     _  Air  Indicated  H.  P. 

Brake  H.  P.   Delivered  to  compressor  shaft. 

This  efficiency  depends  on  the  mechanical  construction 
of  the  compressor  and  the  lubrication.  It  varies  from  80%  to 
92%. 

Compression  Efficiency 

Compression  efficiency  is  the  fatio  of  the  theoretical 
Horse  Power  required  to  compress  an  amount  of  air  to  that 
actually  required  or 

Theoretical  Horse  Power. 

T^      IM   /*  /*\ 

0          Actual  Horse  Power. 


I        AND 

CONDEN 

SERS 

FOR 

EVERY 

S 

ERVICE      ij 

17 


UNION       STEAM       PUMP       COMPANY 


This  efficiency  depends  upon  the  water  jacket  and  cooling 
devices,  and  it  is  principally  to  increase  compression  efficiency 
that  compound  compression  is  employed.  To  determine  the 
compression  efficiency,  the  isothermal  curve  is  plotted  on  the 
air  card  figure  7,  starting  of  course  at  the  beginning  of  the 
stroke  and  ending  at  the  theoretical  delivery  line,  or  thermal 
pressure  line.  The  area  AFDE,  this  divided  by  the  area 
ABDC  of  the  actual  card,  is  the  compression  efficiency.  Actual 
compression  curves  will  follow  the  adiabatic  curve  quite  closely 
as  the  water  jacket  has  little  effect  other  than  to  facilitate 
lubrication. 


Fig.  7. 


Displacement 

Air  compressors  are  always  rated  according  to  displace- 
ment, that  is  the  volume  displaced  by  the  net  area  of  the  com- 
pressor piston. 

Capacity 

The  capacity  should  be  expressed  in  cubic  feet  per  minute 
of  free  air  at  intake  temperature,  and  at  the  pressure  of  dry  air 
at  the  suction. 


PUMPING    MACHINERY.    AIR    COMPRESSORS 

•  »awatf»»v>ttttWvt»^g^-^^w^t^nrTrirrg^^  


18 


|"    BATTLE 

C  REEK. 

MICHIGAN, 

U.  S.A.      ^j] 

Volumetric  Efficiency 

Volumetric  efficiency  is  the  ratio  of  the  actual  number 
of  cubic  feet  of  free  air  compressed  per  unit  of  time  to  the 
number  of  cubic  feet  of  piston  displacement  during  that  time 
or, 

Actual  cubic  feet  of  free  air  per  minute.  f 

v     Cubic  feet  of  piston  displacement  per  minute. 

On  the  indicator  diagram,  the  observed  volumetric  efficiency 
is  jjjf  (fig.  7).  Volumetric  efficiency  depends  upon  the  clearance 
volume  in  the  air  cylinder.  If  there  were  no  clearance  spaces 
in  the  cylinder,  the  volumetric  efficiency  would  be  100%.  The 
greater  the  clearance  volume,  the  greater  -the  volume  of  the 
cylinder  occupied  by  the  expanded  clearance  air.  Volumetric 
efficiency  depends  upon  the  terminal  pressure.  The  higher  the 
terminal  pressure  of  the  air  in  the  cylinder,  the  greater  will 
be  the  volume  occupied  by  the  expanded  air  of  the  clearance 
spaces.  This  means  that  as  the  terminal  pressure  is  in- 
creased, the  volumetric  efficiency  decreases. 

Volumetric  efficiency  depends  upon  the  temperature  and 
pressure  of  the  intake  air.  ;  Since  volumetric  efficiency  refers 
to  free  air  at  14.7  pounds  and  60°  Fah.,  then  every  change  of 
temperature  and  pressure  of  intake  has  its  effect  upon  the 
volumetric  efficiency  of  the  compressor.  For  example,  let  us 
suppose  the  temperature  of  the  intake  air  of  the  compressor 
is  60°  Fah.,  and  the  atmospheric  pressure  14.7  pounds,  or 
in  other  words  it  is  actual  free  air  thai  is  drawn  into  the  cylinder. 
If  the  compressor  has  a  displacement  of  100  cubic  feet  of  free 
air  per  minute,  and  actually  delivers  85  cubic  feet  of  free  air 
per  minute  at  100  pounds  pressure,  the  volumetric  efficiency  is 


Now  if  the  temperature  of  the  intake  air  is  raised  to  65° 
Fah  ,  the  other  conditions  of  operation  remaining  the  same, 
the  compressor  will  still  deliver  85  cubic  feet  of  free  air  per 
minute,  but  owing  to  its  higher  temperature,  a  smaller  weight 
or  mass  of  air  will  be  taken  into  the  cylinder  according  to  the 
law  of  Charles.  85  cubic  feet  of  air  at  60°  Fah.  and  14.7 
pounds  pressure  is  equivalent  to  84  cubic  feet  at  65°  Fah., 
and  14.7  pounds  pressure.  Under  these  conditions  the  volume- 
tric efficiency  decreases 


19 


This  shows  that  there  is  a  loss  of  1%  in  volumetric  effici- 
ency for  every  5  °  rise  in  temperature  of  the  intake  air. 

Volumetric  efficiency  is  also  affected  by  changing  the 
atmosphere  or  intake  pressure,  the  temperature  remaining 
constant.  To  show  this,  assume  that  the  compressor,  referred 
to  above,  were  removed  to  an  altitude  of  5000  feet,  where  the 
intake  air  is  at  12.20  pounds  pressure,  and  60°  Fah.  Now  85 
cubic  feet  of  this  air  is  equivalent  to  70  cubic  feet  of  free  air  at 
sea  level  and  the  volumetric  efficiency  is 


v       100 

In  the  selection  of  air  compressors,  it  should  be  borne  in 
mind  that  they  are  always  rated  according  to  the  piston  dis- 
placement, and  due  allowance  must  be  made  for  the  volumetric 
efficiency.  The  volumetric  efficiency  of  the  average  compres- 
sor varies  from  70%  to  95%  according  to  the  size  and  conditions 
of  operation. 

Compressor  Installation  and  Operation. 

The  large  majority  of  instances  of  unsatisfactory  opera- 
tion of  air  compressors  eminates  from  the  improper  installa- 
tion in  the  first  place,  and  continued  negligent  operation 
and  disregard  of  the  compressor  manufacturer's  instructions 
in  the  second  place.  An  air  compressor  is  looked  upon  by  many 
engineers  as  a  machine  that  can  be  tucked  away  in  an  out-of-way 
place,  and  left  to  itself  without  any  attention. 

An  air  compressor,  like  any  piece  of  machinery,  requires 
some  attention  for  successful  operation,  and  if  the  operator, 
before  erecting  a  compressor,  will  spend  a  little  time  famil- 
iarizing himself  with  the  practical  principles  of  an  air  com- 
pressor, the  biggest  majority  of  the  cases  of  trouble  will  be 
eliminated.  A  careful  study  of  the  compressor  manufacturer's 
instructions  will  enlighten  the  operator  on  this  subject. 

Location. 

An  air  compressor  should  be  installed  in  a  place  which 
is  clean  and  cool,  and  ample  space  be  provided  all  around  the 
compressor  for  cleaning  and  inspecting.  Too  often  compres- 


20 


sors  are  pushed  off  in  a  corner  where  it  is  an  impossibility  to 
get  around  them.  Locations  of  compressors  in  boiler  rooms, 
near  coal  piles,  or  other  places  where  there  is  liable  to  be  an 
accumulation  or  a  settling  of  dust  and  dirt,  should  be  avoided. 

Foundations. 

Air  compressor  foundations  depend  of  course  upon  the  size 
and  type  of  air  compressor,  as  well  as  the  nature  of  the  soil. 

An  air  compressor,  like  an  engine,  requires  a  rigid  founda- 
tion to  prevent  any  vibration.  The  value  of  a  foundation 
made  of  good  materials,  and  well  built,  will  be  readily  under- 
stood. The  slight  difference  in  cost  between  the  best  and 
inferior  materials  and  workmanship  will  save  future  annoy- 
ance and  expense.  The  materials  used  in  the  foundation 
depend  somewhat  upon  local  conditions,  but  it  is  advisable 
to  use  cement  concrete,  as  this  material  furnishes  an  excellent 
foundation  at  a  comparatively  small  cost. 

The  following  mixture  is  recommended  for  concrete 
foundations :  One  part  Portland  cement,  three  parts  coarse  sand 
and  six  parts  broken  stone. 

Allow  the  foundation  to  stand  at  least  a  week  after  it  is 
completed,  before  placing  the  compressor  upon  it. 

With  each  compressor,  the  manufacturer  sends  out  a 
detailed  foundation  plan,  and  the  foundation  can  be  laid  out 
and  built  from  this  plan  before  the  compressor  is  received. 

Air  Inlet  Piping. 

It  has  already  been  shown  that  an  increase  of  5°  Fah.  in 
the  temperature  of  the  intake  air  is  accompanied  by  a  decrease 
of  1%  for  volumetric  efficiency,  which  means  that  as  the  intake 
air  temperature  increases,  the  free  air  capacity  of  the  com- 
pressor decreases,  and  the  same  amount  of  power  is  expended 
as  though  the  full  capacity  of  the  compressor  was  being  realized. 

To  get  the  best  results,  the  air  intake  should  be  piped 
to  the  outside  of  the  building,  some  8  or  10  feet  above  the 
ground  level,  or  above  the  roof.  Dust  and  dirt  must  by  all 
means  be  prevented  from  entering  the  compressor,  as  it  will 
cut  and  wear  the  cylinder  surfaces,  as  well  as  the  valve  seats, 
and  cause  all  manner  of  trouble.  The  intake  opening  should 
be  hooded  to  keep  out  rain,  and  carefully  screened  to  eliminate 
dust  and  dirt. 


AND    CONDENSERS    _FOR   EVERV  SERVICE 

21 


The  intake  pipe  should  be  at  least  the  size  of  the  inlet 
on  the  compressor,  and  wherever  the  line  is  of  any  length,  it  is 
advisable  to  increase  this  size  to  avoid  fractional  losses. 

Discharge  Piping 

The  discharge  pipe  should  be  at  least  the  diameter  of  the 
discharge  opening  in  the  air  cylinder,  and  contain  as  few  bends 
as  possible!  The  discharge  pipe  should  be  carried  the  full  size 
into  the  receiver. 

Air  Receivers 

The  functions  of  an  air  receiver  are  (1)  to  create  a  cushion 
and  eliminate  the  compressor  pulsations  in  the  pipe  line;  (2) 
to  serve  as  a  storage  of  power;  (3)  to  cool  the  air  and  pre- 
cipitate any  oil  or  moisture  in  entrainment;  (4)  to  eliminate 
friction  losses  that  would  occur,  if  cooling  were  effected  in  the 
pipe  lines.  The  receiver  should  therefore  be  located  in  a  cool 
place,  and  as  close  as  possible  to  the  compressor.  The  receiver 
fittings  should  include  pressure  gauge,  safety  valve  and  blow- 
off  cock. 

Lubrication 

Bearings  in  modern  air  compressors,  the  main  bearings 
as  well  as  the  connecting  rod  and  crosshead  bearings,  are  usually 
lubricated  by  means  of  the  splash  system. 


Fig  8. 

The  sectional  view  shown  herewith,  illustrates  an  enclosed 
type  air  compressor  lubricated  by  the  splash  system.  The 
frame  forms  with  its  covers  a  closed  chamber,  with  a  quantity 
of  oil  in  the  basin  below  the  crank,  into  which  the  crank  and 
connecting  rod  dip  at  each  revolution.  The  motion  of  these 
parts  splashes  the  oil  to  every  bearing,  and  insures  copious 
lubrication.  By  means  of  a  well  designed  settling  chamber, 


22 


O 


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ri»«i>i»»vv»»»vv»»^.rWW^rvTr»nl^^^ 


any  sediment  or  abrasive  material,  which  may  accumulate  in  the 
oil,  is  returned  to  the  bottom  of  the  frame,  and  prevented  from 
being  carried  through  the  bearings.  Close  fitting  cast  iron 
covers  prevent  any  leakage  from  the  frame. 

Air  Cylinder:  The  air  cylinder  lubrication  is  by  far  the 
most  vital  point  in  air  compressor  lubrication,  and  as  a  rule  it 
seems  to  be  the  least  understood.  In  order  to  appreciate  the 
necessity  of  proper  cylinder  lubrication,  it  is  advisable  to  con- 
sider the  conditions  that  have  to  be  met. 

The  compression  of  air  results  in  a  rise  in  temperature 
according  to  the  equation  on  page  3.  For  adiabatic  com- 
pression of  air,  the  temperature  and  pressure  relations  are  ex- 
pressed by  the  formula: 

n-i       ,_        _, 

1.29  (18) 


and  Ti  =T    — 


Where  T  and  T1  are  the  initial  and  final  absolute  air  tem- 
peratures, and  P  and  P1  the  initial  and  final  absolute  pressures, 
therefore  the  temperature  of  the  air  at  discharge  from  the 
cylinder  is  dependent  not  only  upon  the  pressure,  but  on  the 
temperature  of  the  intake  air.  For  example,  assume  a  single 
stage  compressor  operating  at  sea  level  at  an  atmospheric 
temperature  of  60°  Fah.,  and  discharging  against  70  pounds 
pressure.  The  final  temperature  then  is: 


or  405°  Fah. 


[84 .  7  ~j  .  29 
w.r] 


866°  absolute 


TABLE   1.     CYLINDER  TEMPERATURES  AT  END  OF  PISTON  STROKE. 


Final 
Pressure 
of  Air 
Lb.  Gage 

Final  Temperature 
Deg.  F. 

Final 
Pressure 
of  Air 
Lb.  Gage 

Final  Temperature 
Deg.  F. 

Single-Stage 

Two-Stage 

Single-Stage 

Two-Stage 

10 
20 
30 
40 
50 
60 
70 
80 
90 

145 
207 
255 
302 
339 
375 
405 
432 
459 

*  '"  i 

188 
203 
214 
224 
234 

100 
110 
120 
^130 
140 
150 
200 
250 

485 
507 
529 
550 
570 
589 
672 
749 

243 
250 
257 
205 
272 
279 
309 

sal 

AND    CON  D  E  N  S  E  R  S    F  O  R    EVE  RY   S  E  RV I C  E 


23 


I 


This  calculation  does  not  take  into  consideration  jacket 
cooling,  or  heat  radiation,  so  in  practice  the  actual  discharge 
temperature  will  be  slightly  less.  The  foregoing  table  gives 
the  cylinder  temperature,  in  single  and  two  stage  compression 
for  pressures  from  10  pounds  up  to  250  pounds  gauge. 

For  successful  lubrication  of  the  air  cylinders,  it  is  neces- 
sary to  use  oil  which  reduces  the  friction  to  a  minimum,  and 
eliminates  carbonization  as  much  as  possible.  Carbonization 
is  generally  caused  by  using  a  poor  grade  of  oil,  such  as  steam 
cylinder  oil,  which  is  easily  decomposed  by  the  heat  of  com- 
pression, or  the  use  of  too  great  a  quantity  of  oil,  or  the  failure 
to  properly  screen  the  intake  pipe  of  the  compressor,  thus 
permitting  dust  and  foreign  matter  to  enter  the  air  cylinder. 

Air  cylinder  oil  should  be  a  medium  body  pure  mineral  oil 
of  either  a  paraffin-base  or  asphal tic-base. 

With  the  paraffin-base  oil,  any  carbon  deposit  is  very 
adhesive,  and  of  a  hard  flinty  material ;  while  with  the  asphal  tic- 
base  oil,  the  carbon  deposit  is  of  a  light  fluffy  nature,  and  easily 
cleaned  out. 

The  following  tables  published  by  the  Compressed  Air 
Society  will  serve  as  a  guide  to  specify  the  qualities  to  be  posses- 
sed by  an  oil  for  air  cylinder  lubrication. 

The  average  range  of  figures  are  recommended  for  single 
stage  compression  up  to  100  pounds  pressure,  and  for  two 
stage  air  compression  for  higher  pressures  in  which  the  air  is 
cooled  between  stages  so  that  the  maximum  terminal  tem- 
perature is  not  in  excess  of  that  due  to  a  pressure  of  100  pounds 
for  a  single  stage  compressor. 

TABLE  II.     PHYSICAL  TESTS  OF  PARAFFIN-BASE  OILS. 

Minimum  Average  Maximum 

Gravity,  Baume 28  to     32  deg.  25  to     30  deg.  25  to     27  deg. 

Flash  point,  open  cup 375  to   400  deg.  F.  400  to  425  deg.  F  425  to   500  deg.  F 

Fire  point 425  to  450  deg.  F    450  to   475  deg.  F  475  to   575  deg.   F 

Viscosity  (Saybolt)  at  100 

deg.  F 120  to   180  sec.          230  to   315  sec.  to   1500  sec. 

Color Yellowish  Reddish  Dark  red  to  green 

Congealing  point  (pour  test)    20  to     25  deg.  F    30  deg.  F.  30  to     45  deg.  F 

TABLE  III.     PHYSICAL  TESTS  OF  ASPHALTIC-BASE  OILS 

Minimum  Average  Maximum 

Gravity,  Baum«f. 20  to     22  deg.  F  19.8  to  21  deg.F  19.  5  to  20.  5  deg.  F- 

Flash  point,  open  cup 305  to  325  deg.  F  315  to  335  deg.  F  330  to  375  deg.  F 

Fire  Point 360  to   380  deg.  F  370  to  400  deg.  F  385  to  440  deg.  F 

Viscosity  (Saybolt)  at  100 

deg.  F 175  to  225  sec.  275  to   325  sec.  475  to   750  sec. 

Color Pale  yellow  Pale  yellow  Pale  yellow 

Congealing  point  (pour  test)  0  deg.  F.  0  deg.  F.  0  deg.   F. 


J"       PUMPING 

MACHINERY, 

AIR. 

COMPRESSORS 

3 

24 


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C  REEK. 

MICHIGAN, 

U.  5 

>.  A.       : 

Quantity  of  Lubricating  Oil  for  Air  Cylinders 

The  proper  quantity  of  lubricating  oil  to  be  used  in  the 
air  cylinders  depends  upon  the  viscosity  of  the  oil,  but  it  should 
be  borne  in  mind  that  when  the  surface  of  the  cylinder  wall  is 
once  glazed  over,  little  oil  is  required  to  lubricate  the  surfaces. 
The  following  table  shows  the  approximate  quantity  of  oil  for 
air  cylinder  lubrication: 

TABLE  IV.     QUANTITY  OP  AIR-CYLINDER  LUBRICANT  REQUIRED 
PER  10-HOUR  DAY. 


Size  of 
Cylinder, 
Inches 

Displace- 
ment per 
Minute 
Cu.  Ft. 

Piston 
Speed, 
Feet  per 
Minute 

Sq.  Ft.  of 
Cyl.  Wall 
Swept  by 
Piston 

°nu 

tn  <u  +-> 

l«l 

QOS 

Drops 
of  Oil 
per  10 
Hours 

Sq.  Ft. 
Oiled 
per  Drop 

Pints  of 
Oil  per 
10  Hours 

6^x  6 

57 

330 

440 

1 

600 

440 

.0375 

8x  8 

124 

354 

740 

2 

1200 

370 

.0750 

10x10 

228 

416 

1095 

2 

1200 

548 

.0750 

12x12 

371 

470 

1480 

3 

1800 

493 

.1125 

14x15 

561 

525 

1930 

4 

2400 

483 

.1500 

16x15 

730 

525 

2200 

4 

2400 

550 

.1500 

18x15 

930 

525 

2480 

5 

3000 

496 

.1875 

20x15 

1146 

525 

2770 

6 

3600 

462 

.2250 

Steam  Cylinder  Lubrication 

The  steam  cylinder  of  the  compressor  requires  a  good 
grade  of  steam  cylinder  oil,  and  due  to  its  constant  washing 
away  by  the  steam,  it  should  be  fed  to  the  cylinder  in  greater 
quantities  than  in  the  air  cylinder. 

The  following  table  gives  the  approximate  quantity  of 
oil  for  steam  cylinder  lubrication. 

TABLE  V.     OIL  REQUIRED  FOR  STEAM-CYLINDER  LUBRICATION. 


Size  of  Cylinder, 
Inches 

6'Vgx  6 
8x8 
10  xlO 
12  x!2 
14  x!5 
16  xlO 
18  x!5 
20  x!2 
24  x!5 


Drops  of  Oil 
per  Minute 

3 

4 

6 

8 
11 
11 
14 
14 
20 


Pints  of  Oil  per 
10  Hours 

.3 

.4 

.6 

.8 
1.1 
1.1 
1.4 
1.4 
2  0 


Inspection  and  Cleaning  of  Air  Compressors 

At  stated  intervals,  say  once  a  month,  the  compressor 
should  be  carefully  inspected,  lost  motion  in  bearings  taken 
up,  and  any  defect  corrected. 


25 


UNION       STEAM       PUMP       COMPANY 


1 


The  best  of  lubricating  oils  will  cause  a  deposit  of  carbon 
In  the  compressor  system,  and  for  this  reason  the  air  cylinder 
should  be  cleaned  occasionally  probably  once  a  month,  by 
filling  the  lubricator  with  a  strong  solution  of  water  and  soap, 
and  feeding  liberally  during  a  day's  run.  Careful  attention 
to  this  will  avoid  an  accumulation  of  carbon  in  the  cylinder 
and  pipe  line. 

The  oil  in  the  crank  case  should  be  drawn  out  once  a 
month,  and  the  frame  thoroughly  washed  out  with  kerosene, 
and  then  wiped  out  clean  with  a  cloth.  The  oil  may  be  used 
over  again  if  it  is  properly  filtered. 

Circulating  Water 

The  duty  of  the  jacket  water  is  to  carry  off  the  heat  of 
compression,  and  to  do  this  successfully  requires  that  the  supply 
of  cooling  water  be  liberal.  The  air  cylinders  are  provided 
with  water  inlet  openings  at  the  bottom,  and  the  outlet  at  the 
top.  The  water  outlet  should  be  in  plain  view  of  the  operator 
to  insure  that  the  water  is  circulating,  and  it  is  best  to  arrange 
this  by  allowing  the  water  to  flow  into  an  open  funnel. 

General  Construction  of  Air  Compressors. 

In  the  modern  air  compressor,  the  frames  are  of  the  enclosed 
type,  and  are  of  either  the  center  crank  or  side  crank  design. 
The  center  crank  design  illustrated  in  Fig.  9  is  used  on  single 
compressors.  The  side  crank  design  illustrated  in  Fig.  10  is 
of  the  rolling  mill  type,  and  is  used  only  on  duplex  compressors. 


Fig.  9. 


JULJJ^Tm!^3gi^-'rT^^E?1Cy»^^ 

PUMP  IN  G    MAC  H I NJE  RY;__.  AIKL_  CO  MPRJLSS_QR  S 

.T~ ...  „.  ^  «.  uu  ^uTS^L  ww  w  w  w -ju-w  w  vrarvtna-  w  Vtf'w  tf  W  W  ffl.B XX  W  W  Tfr  nry  m  a  g^Tfl  lf\rtnr& IfiTW  ft  tf  IT VitfWVi W  W WYWf.'Srfni  M ? 


26 


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M 

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U. 

s. 

A. 

J 

The  frames  are  of  massive  proportion  with  metal  properly 
distributed  to  secure  the  maximum  strength  and  rigidity. 
They  are  extended  to  the  foundation  in  the  form  of  a  broad, 
liberal  support  reaching  their  entire  length.  The  crosshead 
guides  are  bored  at  the  same  setting  as  the  fittings  for  the 
cylinders,  thus  insuring  perfect  alignment. 


Fig.  10. 


All  bearings  are  lubricated  by  the  splash  system  from 
the  main  frame.  Close  fitting  cast  iron  covers  prevent  any 
leakage  from  the  frame. 


Fig.  11. 


Crank  Shaft. 

The  crank  shaft  is  made  of  high  carbon  steel,  ana  is  ac- 
curately finished  and  ground  to  size. 

On    single    compressors    and    small    duplex    compressors, 


UNION       S  T  E  AM       PUMP       COM  P  ANY 


the  shaft  is  of  the  center  crank  type  with  counter    weights 
securely  fastened  to  each  crank. 


Fig.  12. 


On  duplex  compressors,  the  shaft  is  fitted  with  heavy 
balanced  crank  discs,  which  are  forced  on  to  the  shaft  by 
hydraulic  pressure,  and  securely  held  in  place  by  means  of 
carefully  fitted  keys.  The  crank  fins,  which  are  of  carbon 
steel,  are  finished,  ground  to  size,  and  pressed  into  the  crank 
discs,  after  which  they  are  riveted  over  on  the  back. 


Connecting  Rod 

The  connecting  rod  is  a  high  grade  Hammered  steel  forging. 
It  is  fitted  with  bronze  box  in  the  crosshead  pin  end,  and  babbitt 
lined  bronze  box  in  crank  pin  end.  Wedge  adjustment  to  com- 
pensate for  wear  is  provided  for  both  boxes.  The  bearing  boxes 
are  designed  with  liberal  proportions,  insuring  low  bearing 
pressures  per  square  inch. 


Fig.  13. 


28 


„ . .  .„  „ „ . „ „      „ .^g^^       MICHIGAN,      U.  S.  A. 

••»»•»»»»»  at  »»wir»»«uw»«»»V»«»««»i»iii«»»»»i»*»»»»re»^^ 


Crosshead 

The  crosshead  is  a  steel  casting  and  is  provided  with  ad- 
justable parallel-fitted  bronze  shoes  top  and  bottom.  It  has 
unusual  large  bearing  surface  and  the  bearing  pressure  per 
square  inch  is  correspondingly  low. 

Crosshead  pin  is  made  of  best  grade  carbon  steel  and  is 
accurately  finished,  hardened  and  ground.  It  is  fitted  into 
the  crosshead  on  a  taper  and  is  secured  by  a  nut  and  a  lock  nut. 


Fig.  14. 


AND    CONDENSERS    FOR   EVERT   SERVICE 


Air  Valves 


Fig.  226. 
Discharge  Valve  Parts. 


Fig.  227.    Suction  Valve  Parts. 


Fig.  228. 
Suction  Valve  Parts  Used  on  Class  "BL"  Air  Compressors. 


30 


The  valves  and  their  arrangement  are  the  most  vital  parts 
in  the  construction  of  an  air  compressor.  No  pains  have  been 
spared  to  make  these  parts  of  the  best  quality  and  design.  Both 
suction  and  discharge  valves  are  of  the  flat-disc  type  and  are 
made  of  special  grade,  heat-treated  steel,  ground  to  size.  Suc- 
tion and  discharge  valves  are  of  the  same  size  and  interchange- 
able. These  valves  which  with  their  seats  and  guards  consti- 
tute single  units,  are  easily  accessible  by  the  removal  of  screwed 
caps.  The  valve-seats  are  of  the  double-ported  type,  which 
arrangement  gives  a  maximum  opening  with  very  slight  lift  of 
valve.  These  features  practically  eliminate  all  noise  of  opera- 
tion and  insure  a  long  life  of  the  valve  at  high  speeds. 


Fig.  19. 

Air-Cylinder  Section,  Showing  Piston  Construction, 
Valves,  Water-Jacketing  Spaces. 


|  "AND 

CONDENSERS 

FOR 

EVERY 

SERVICE 

31 


|        UNION 

STEAM 

P  UMP 

COM  PANY 

J 

Air-Cylinders. 

The  air-cylinders  are  made  of  semi-steel,  ccmnterbored  at 
the  ends,  and  have  water  jackets  extending  entirely  around 
cylinders.  Both  heads  are  also  water- jacketed,  and  special 
attention  has  been  paid  to  the  circulation  of  the  cooling  water, 
in  order  to  get  the  maximuni  cooling  effect  with  the  least  amount 
of  water.  With  the  object  of  making  the  volumetric  efficiency 


Fig.  20. 

as  high  as  possible,  the  clearance  spaces  have  been  reduced  to  a 
positive  minimum.  Sufficient  space  is  allowed  for  the  passage 
of  the  air,  and  not  a  cubic  inch  more  than  is  necessary. 

The  air-pistons  are  of  semi-steel,  each  with  two  carefully 
fitted  snap  rings.  Pistons  are  fastened  to  piston  rods  by  taper 
and  nuts. 

Valve  Gear. 

On  steam-driven  compressors,  the  steam  valves  are 
operated  by  eccentrics  on  the  crank-shaft.  These  eccentrics 
are  lubricated  from  the  crank-case,  thus  avoiding  the  use  of 
any  grease  or  oil  cups.  The  valve-gears  with  the  fewest  num- 


32 


I 

B 

ATTLE 

C 

RE 

EK. 

MIC 

HIG 

AN. 

U.  5 

>.  A. 

3 

ber  of  working  parts  possible,  are  coupled  direct,  avoiding 
any  offsets  or  the  use  of  rock  arms,  which  may  give  trouble. 
Take-up  for  wear  is  provided  at  every  bearing. 

Steam  Cylinders. 

The  steam  cylinders  which  are  made  of  semi-steel,  are 
amply  heavy  to  permit  of  reboring.  They  are  counterbored 
at  the  ends  to  prevent  the  rings  wearing  a  shoulder,  and  are 


Fig.  21. 


lagged  with  black  iron.  The  steam  chests  are  cast  integral 
with  the  cylinders.  The  steam  openings  are  short  and  direct, 
and  are  properly  proportioned  to  avoid  any  wire  drawing  of 
steam,  and  reduce  clearance  to  a  minimum 

The  steam-cylinders  are  equipped  with  flat-faced  slide 
valves,  and  cylinders  10  x  10  and  largef  have  balancing  pistons 
to  balance  the  steam  pressure  on  the  back  of  the  main  valve 
to  reduce  the  friction  and  wear  to  a  minimum.  Compressors 
with  12  x  12  steam-cylinders  and  larger  have  the  Meyer  cut- 
off adjustable  to  give  cut-off  from  one-quarter  to  three-quarter 
stroke. 


|       AND 

CONDENSERS 

FOR 

EVERY 

SERVICE     ^J 

33 


STEAM       P  U  M  P       C  6  M  P  AN  Y 


PUMPING   MACHINERY,    AIR   COMPRESSORS 


34 


s  3 
y 


AND   CONDENSERS    FOR   EVERY  S 


35 


U  N 

1  O 

N 

S  T 

E  A,M 

P 

UM 

P 

C 

OM 

PANY 

3 

Classification  of  Air  Compressors 

Air   compressors   are   classified   according  to   their   design 
as  follows: 

Straight  Line  Steam  Driven. 

Simple  Steam  Single  Stage  Air. 

Simple  Steam  Two  Stage  Air. 
Straight  Line  Power  Driven. 

Single  Stage. 

Two  Stage. 
Duplex  Steam  Driven. 

Simple  steam  single  stage  air. 

Compound  steam  single  stage  air. 

Simple  steam  two  stage  air. 

Compound  steam  two  stage  air. 
Duplex  Power  Driven. 

Single  stage  air. 

Two  stage  air, 


Types  of  Drive 

Air  Compressors  are  classified  according  to  the  type  of  drive 
into  steam  driven. and  power  driven. 

The  regular  steam  driven  air  compressor  consists  of  a  very 
efficient  steam  engine  with  one  or  more  air  cylinders  directly 
coupled  on  the  extended  piston  rod. 

In  this  type  of  compressor,  the  power  is  transmitted  direct, 
and  transmission  losses  are  reduced  to  the  minimum. 

Steam  driven  compressors  may  be  fitted  with  either  simple 
or  compound  steam  cylinders,  depending  upon  the  conditions. 
Compound  steam  cylinders  are  recommended  for  steam  pres- 
sures as  low  as  80  pounds,  operating  condensing,  and  for  100 
pounds  operating  non-condensing. 

Power  driven  air  compressors  comprise  the  plain  belt  drive, 
the  short  belt  drive,  the  gear  drive,  and  the  silent  chain  drive. 

The  plain  belt  drive  is  probably  the  most  common  method 
used  in  driving  power  air  compressors,  and  this  is  a  practical 
type  of  drive  where  there  is  ample  space  to  get  a  sufficient 
center  distance  between  the  compressor  pulley,  and  the  motor. 
This  center  distance  should  be  three  to  four  times  the  diameter 
of  the  compressor  pulley,  and  the  direction  of  the  belt  motion 
should  be  such  as  to  put  the  slack  on  top. 


!^.^ 

36 


Where  ample  belt  centers  cannot  be  obtained,  the  short 
belt  drive  is  advisable.  This  arrangement  consists  of  a  floating 
idler  pulley  and  a  very  short  belt.  The  weight  of  the  idler  takes 
up  the  slack  of  the  belt,  and  increases  the  arc  of  contact  on  the 
driving  and  driven  pulleys,  so  that  the  full  power  is  transmitted 
without  any  undue  strain  on  the  bearings,  or  belt  itself. 

The  short  belt  drive  is  recommended  as  the  most  satis- 
factory type  of  drive  for  a  power  driven  air  compressor. 

The  gear  drive,  and  the  silent  chain  drive  are  never  advis- 
able, and  should  be  used  only  on  very  small  units  where  the  de- 
mand for  compactness  renders  them  imperative. 

Steam  Consumption  of  Air  Compressors 

The  steam  consumption  of  an  air  compressor  varies  with 
the  type  and  size  of  machine,  and  the  conditions  of  operation. 

The  following  table  will  give  an  idea  of  the  approximate 
steam  consumption  of  air  compressors  of  different  sizes  with 
simple  and  compound  steam  cylinders. 

Table  of  Steam  Consumption  of  Air  Compressors 

Simple  Steam  Cylinders. 

Steam  per  I.  II.  P.  per  hour,  non- 
condensing,  100-125  pounds 
Size  of  Cylinders  steam  pressure. 


x    6  46 

8x8  42 

10      x  10  40 

12      x  12  33 

14      x  15  30 

16      x  15  29 

18      x  15  28 

Compound  Steam  Cylinders. 


Steam  per  I.  H.  P.  per  hour,  non- 
condensing,  100-125  pounds 


Size  of  Cylinders 

steam  pressure. 

8  and  12  x    8 

30 

10  and  16  x  10 

28 

12  and  20  x  12 

26 

14  and  24  x  15 

25 

|       AND    CONDENSERS 

FOR    EVERY  SERVICE      ^ 

37 

3LJLJLJLJULJLJIA*  *a  AftRflJUJ)  a«  ««  .  u  Tmnrnra  innt  u  a  a  .  n  .  « 


UNION       STEAM       PUMP       COM  P  ANY 


Indicated  or  Brake  Horse  Power  of  an  Air 
Compressor 

The  method  of  calculating  the  theoretical  horse  power  to 
compress  air  by  single  stage  and  two  stage  compression  has 
already  been  shown,  and  on  pages  66  and  67,  the  theoretical 
horse  power  for  various  pressures  in  one,  two,  three  and  four 
stage  compression  is  tabulated. 

The  theoretical  figures  given  do  not  take  into  consideration 
the  losses  in  the  air  cylinders  due  to  clearance,  the  heat  of  com- 
pression, etc.,  nor  the  mechanical  losses  in  'the  operation  of  the 
compressor.  Consequently,  to  arrive  at  the  indicated  or  brake 
horse  power  to  compress  a  cubic  foot  of  free  air,  it  is  necessary 
to  take  the  indicated  horse  power  of  a  steam  driven  compressor, 
and  the  brake  horse  power  of  a  power  driven  compressor,  and 
measure  the  actual  free  air  delivered  corrected  to  the  suction 
temperature  and  pressure. 

The  indicated  or  brake  horse  power  to  compress  a  cubic 
foot  of  free  air  may  then  be  accurately  determined,  and  all 
losses  are  taken  into  consideration. 

Due  to  these  varying  conditions  in  the  compression  of  air, 
it  is  a  more  convenient  method  of  calculation  to  base  the  indi- 
cated or  brake  horse  power  on  the  displacement  of  the  com- 
pressor. 

The  following  tables  give  the  approximate  indicated  or 
brake  horse  power  to  compress  air  by  single  or  two-stage  com- 
pression per  cubic  foot  of  compressor  displacement.  In  compar- 
ing the  horse  power  figures  for  single  and  two-stage  compression, 
it  should  be  borne  ^in  mind  that  a  two-stage  compressor  has  a 
higher  volumetric  efficiency  than  a  single-stage  machine. 

Approximate  Indicated  or  Brake  Horse   Power  to   Compress   1  Cubic  Foot  of  Com- 
pressor Displacement  per  Minute  by  Single  Stage  Compression  at  Sea  Level. 


Gauge 
Pressure 

Horse 
Power 

Gauge 
Pressure 

Horse 
Power 

Gauge 
Pressure 

Horse 
Power 

5 

.0235 

45 

.124 

85 

.160 

10 

.0435 

50 

.130 

90 

.167 

15 

.062 

55 

.132 

95 

.172 

20 

.0756 

60 

.135 

100 

.178 

25 

.090 

65 

.143 

105 

.182 

30 

.102 

70 

.150 

110 

.190 

35 

.112 

75 

.155 

125 

.206 

40 

.12 

80 

.158 

Approximate  Indicated  or  Brake  Horse  Power  to   Compress   1  Cubic  Foot  of  Com- 
pressor Displacement  per  Minute  by  Two  Stage  Compression  at  Sea  Level. 


Gauge  Pressure 

Horse  Power 

Gauge  Pressure 

Horse  Power 

80 

.157 

300 

.288 

90 

.165 

350 

.305 

100 

.177 

400 

.319 

125 

.189 

450 

.332 

150 

.210 

500 

.345 

175 

.221 

200 

.242 

250 

.265 

MACHINERY    AIR   COMPRESSORS 


Fig.  25.     Class  "SL"  Steam-Driven 


Fig.  24.     Class  "BL"  Belt-Driven      •  .Fig.  2 

Air  Compressor,  Enclosed  Type.  Air  Compressor,  Enclosed  Type. 

Class  "BL"  Belt-Driven  Air  Compressors,  Enclosed  Type. 


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AND    CONDEN  SJERS_  F OR    EVE RY1 S  E RVI C E 

39 


§2     UNION 

STEAM 

P  UMP 

COM  P  ANY 

4 

Fig.  136 

Class   "TTBL"    Belt- Driven 

Air  Compressor,  Double- Acting 

Two- Stage,  Enclosed  Type. 


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Fig.  187 

Class  "TTSL"  Steam- 

Driven  Double- Acting 

Two-Stage  Compressor. 

Enclosed  Type. 


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High  Pressure  Duplex  Belt  Driven  Gas  Compressors 
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Fig.  28. 


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UNION       STEAM       PUMP       COMPANY 


Fig.  30b 
Class  "DSL"  Duplex  Steam-Driven  Center  Crank  Air  Compressors,  Enclosed  Type.  Fig.  30a 


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V 

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Fig.  31 


Class  "DBTL"  Duplex  Two-Stage,  Short-Belt  Driven,  Center  Crank  Air  Compressor, 
Enclosed  Type.     Fig.  31. 


Size  of 
Compressor 

CAPACITY 

Driving 
Pulley 

Size  of  Opening 

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u 

V 

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Free  Air 

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Duplex  Two-Stage,  Short  Belt-Driven,  Side  Crank  Air  Compressor, 
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Size  of 

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CAPACITY 

Driving 
Pulley 

Size  of  Openings 

I 

VI 
3  (U 

11 
II 

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Cu.  ft.  Free  Air. 

ll 
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10 
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12 
12 
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15 
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250 
250 
250 
235 
235 
235 
210 
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1.310 
1.310 
1.780 
1.780 
2.800 
3.540 
3.540 
4.420 
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325 
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125 
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54 
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Pig.  33a 


"DSTL"  Duplex  Two-Stage.  Steam- Driven  Center  Crank  Air  Compressor, 
Enclosed  Type  Fig.  33a 


SIZE  OF 

CAPACITY 

Size  of  Openings 

COMPRESSOR 

Displacrm't 

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E 

E 

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a 

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Cylinders 

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Pressure 

Indicated  He 
at  100  Pound 
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1 

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8 

12 

7 

8 

265 

1  .05 

278 

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110 

46 

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Class  "SDT"  Duplex  Two-Stage,  Steam-Driven  Side  Crank  Air  Compressor, 
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SIZE  OF 
COMPRESSOR 


8 

8 
10 
10 

12 
12 
12 


CAPACITY 


II 

250 
250 
250 
250 
235 
235 
235 
210 
210 


Displacem't 
Cubic  Feet 
Free  Air 


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.78 
.80 
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325 
325 
445 
445 
655 
830 
830 
929 
1146 


150 
12o 
150 
125 
1501  115 
150  100 
100  100 
125  85 
3251  100. 


54 

54 

74 

71 

110 

139 

139 

155 

190 


Size  of  Openings 


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at  compressor 


B 

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LE 

C 

REEK, 

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G 

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Fig.  34 

Class  "CTD"  Duplex  Cross  Compound,  Two-Stage,  Side  Crank,  Air  Compressor, 
Enclosed  Type 


SIZE  OF  COMPRESSOR 

CAPACITY 

SIZE  OF  OPENINGS 

Diam.  of  High  Pres- 
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Diam.  of  Low  Pres- 
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1 

Pu  £ 

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j 

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10 
12 
12 
12 
14 
14 

16 
16 
16 
16 
20 
20 
20 
24 
24 

12 
12 
14 
14 
16 
18 
18 
18 
20 

7 
8 
7 
8 
10 
10 
12 
12 
12 

10 
10 
10 
10 
12 
12 
12 
15 
15 

250 
250 
250 
250 
235 
235 
235 
210 
210 

1.31 
1.31 
1.78 
1.78 
2.79 
3.54 
3.54 
4.42 
5.45 

325 
325 
445 
445 
656 
831 
831 
929 
1146 

150 
125 
150 
125 
150 
150 
100 
125 
125 

90 
80 
115 
110 
100 
110 
100 
85 

100; 

54 
54 

74 
74 
110 
139 
1391 
155 
190 

3 
3 
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4 

5 
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5 
6 
6 
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8 
8 

4 

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4^ 
5 
6 
6 
6 
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11A 
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Fig.  35 

Vertical  Duplex  High-Speed  Air  Compressors 


Fig.  36. 
Vertical  Single  High-Speed  Air  Compressors. 


AND    CONDENSERS    FOR   EVERY  SERVICE 


45 


UN 

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STEAM 

P  UM  P 

C  OMPATfl 

23 

Union  Vertical  Water-Cooled  Air  Compressors 


SIZE 
Bore  and 
Stroke 

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SPEED 
R.  P.  M. 
Min.        Max. 

Displacement  cu.  ft. 
Free  Air  per  minute 
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Pressure 
Designed  for 

1  Brake  H.  P.  required 
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01  £=  Maximum  Speed 

Openings 

Fly-Wheel 

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300  -450 
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275  -400 

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42 
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140 

200 
150 
125 
125 

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2 

150 

2300 

1100 

54 

12 

A 

T« 

6 

2H 

191 

3000 

1700 

165  pounds  hydraulic  test  pressure;  110  pounds  working  pressure. 


PUMPING    MACHINERY,    AIR   COMPRESSORS 


46 


BATTLE      CREEK.     MICHIGAN,     U.S.A. 


USES  OF  COMPRESSED  AIR 

New  uses  are  being  found  every  day  for  compressed  air. 
The  following  list  shows  a  few  of  the  many  applications  of 
compressed  air,  which  will  serve  as  a  guide  to  those  contem- 
plating its  use. 


ACID  WORKS 

Agitating,  Elevating  and    Trans- 
ferring Acids  and  Acid  Solutions 
Pumping  Water 

ASPHALT  REFINERIES 

Agitating  Asphalt 

Scaling  Asphalt  Tanks  or  Vats 

AGRICULTURAL  IMPLE- 
MENT MAKERS 

Operating    Pneumatic    Hammers 
and  Drills 

Running   Pneumatic    Hoists    and 
Lifts 

Sand  Blast  for  Cleaning  Castings 
and  Removing  Paint 

Pneumatic   Painting  and  White- 
washing 

Blowing  Oil  Furnaces 

Cleaning  Boiler  Tubes 

AUTOMOBILE  GARAGES  AND 

REPAIR  SHOPS 
Pumping  up  Tires 
Cleaning    Engines    and    Machines 

by  the  Air  Jet 

Operating  Jacks,  Lifts  and  Hoists 
Running     Pneumatic     Hammers, 

Drills,  Reamers,  etc. 
Cleaning  Cars  and  Cushions  with 

the  Air  Jet 

Operating   Brazing  Forges 
Supplying  Oil  Burners 
Starting  Gas  and  Gasoline  Engines 

BLEACHERIES 

Pumping  Water 

Handling   Chlorine   or    Bleaching 

Solutions 
Agitating  Liquids 

BOILER  SHOPS 

Running  Chipping,  Riveting  and 

Calking  Hammers 
Operating   Drills,   Reamers,    Flue 

Rollers,   Flue  Expanders,   Stay 

Bolt  Cutters,  Punches,  etc. 
Blowing  Rivet  Forges 
Supplying  Hoists,  Lifts  and  Jacks 
Cleaning  Boiler  Flues 
Removing  Scale,  Rust  and  Paint 

by  the  Sand  Blast 


BREWERIES 

Pumping  Water 

Racking  Beer 

Scaling  Condenser  Coils 

Cleaning  Boiler  Tubes 

Cleaning  Machines  by  the  Air  Jet 

Operating  Air  Hoists  and  Lifts 

Refrigeration 

BRIDGE  BUILDERS 
Operating  Chipping  and  Riveting 

Hammers,   Drills,  Reamers, 

Punches,  etc. 

Supplying   Air   Hoists   and   Lifts 
Blowing  Rivet  Forges 
Cleaning    Steel    with    the    Sand 

Blast 
Pneumatic     Paint     Spraying 

System 

CEMENT  BLOCK  FACTORIES 

Operating  Sand  Sifters 
Running    Concrete    Rammers 
Air  Hoists  and  Lifts 

CEMENT  LAKES 
Pumping  Marl  or  Slurry  by  the 
Return-Air  System 

CEMENT  MINES  OR 

QUARRIES 
Operating  Rock  Drills 

CHEMICAL  WORKS 

Pumping  Water 

Agitating,   Aerating,   Elevating 

and  Transferring  Liquids 
Testing  and  Calking  Tanks   and 

Pipe  Lines 

CHINA  WORKS  AND 

POTTERIES 
Spraying  Colors  and  Enamels 

COAL  MINES 

Operating  Coal  Punchers,  Chain 
Machines  and  Coal  Cutters 

Running  Rock  Drills  and  Ham- 
mer Drills 

Pneumatic  Haulage  Systems 

Return  Air  System  for  Station 
and  Sump  Pumping 


AND    CONDENSERS    FOR   EVERY  SERVICE 


47 


UNION       STEAM       PU  M  P       COM  P  ANY 


1 


Operating    Direct-Acting    Pumps 
Running    Coal    Pick    and     Drill 

Sharpeners 
Cleaning  Boiler  Flues 
Pneumatic  Tools  for  the  Repair 

Shop 

Air  Hoists,  Lifts  and  Motors 
Pile  Drivers  for  Shaft  Sinking 
Air  Lift  Pump  for  Water  Supply 

or  Mine  Unwatering 

CONTRACT  WORK 

Running    Rock    Drills,    Hammer 

Drills  and  Stone  Channelers 
Operating   Pneumatic   Hammers, 

Drills  and  Reamers 
Calking  Pipe  Lines  and  Tanks 
Running  Pumps 
Plug  Drills  in  Trenching 
Sheet  Pile  Drivers 
Drill  Sharpeners 
Blowing  Smith  Fires 
Submarine  Drills 
Subaqueous  Tunneling 
Caisson  Work 
Steam  Shovels 

COTTON  FINISHING  WORKS 

Pumping  Water 

Operating  Baling  Presses 

Cleaning  Presses,  Slashers,  and 
other  Machines  by  the  Air  Jet 

Agitating,  Elevating  and  Trans- 
ferring Dyes  and  Solutions 

Air  Hoists,  Lifts  and  Motors 

Automatic    Sprinkler    Systems 

Humidifying  Systems 

COTTON  MILLS 

Pumping  Water 

Cleaning  Looms,  Lifts  and  Spindle 

Rails  by  the  Air  Jet 
Humidifying  Systems 
Automatic   Sprinkler  Systems 
Air  Lifts,  Hoists  and  Motors 
Moistening  Goods 

COTTON  OIL  MILLS 

Cleaning  Crusher   Rolls   and 

Separator  Plates 
Air  Hoists,  Lifts  and  Motors 
Pumping  Water 
Operating  Formers 

CREOSOTING  PLANTS 
Wood  Preserving  Processes 

CUT  STONE  AND  MONUMEN- 
TAL YARDS 

Running  Stone  Tools,  Polishers, 
etc. 


Lettering  and  Carving 
Cleaning,  Carvings  with  the  Air 

Jet 

Air  Hoists  and  Lifts 
Running  Plug  Drills  and  Brush 

Hammers 

•DYE  WORKS 

Pumping  Water 

Agitating,  Elevating  and  Trans- 
ferring Dyes 

ELECTRIC  POWER  AND 
LIGHTING  PLANTS 

Operating  Air  Hoists 

Cleaning  Engines  and  Generators 

with  the  Air  Jet 
Cleaning  Boiler  Flues 
Calking  Boilers 

ELECTRIC  RAILWAYS 

Cleaning  Motors  and  Generators 

with  the  Air  Jet 

Pneumatic   Hammers   and    Drills 
Air  Hoists,  Lifts  and  Jacks 
Blowing  Forges 
Cleaning  Cars  by  the  Air  Jet 
Pumping  Water 
Air  Brakes 

Storage  Air  Brake  Systems 
Switch  and  Signal  Systems 
Operating  Car  Doors. 
Track  Sanders 
Cleaning  Rails  by  the  Sand  Blast 

Preliminary  to  Electric  Welding 

ENAMELED   IRON  WORKS 
Blowing  or  Spraying  Enamel 

FIRE  STATIONS 

Blowing  Fire  Whistles 

Pumping  Water 
Cleaning,  with  the  Air  Jet 
Cleaning  Boiler  Flues 

FOUNDRIES 

Operating    Sand    Rammers    and 

Molding  Machines 
Pneumatic    Hammers   and    Drills 
Pneumatic  Sand  Sifter 
Air  Hoists,  Lifts  and  Motors 
Cleaning    Castings   by   the    Sand 

Blast 

Blowing  Out  Cores 
Drilling  Salamanders 
Aerating  Metal  in  Bessemer 

Process 


JL_B 

ATTLE 

C 

REE 

K. 

M 

ICH 

I  CAN, 

U. 

S. 

A. 

4 

GAS  WORKS 
Starting  Gas  Engines 
Compressing   Carbonic   Acid 
Acetylene,     Oxygen     and     other 

Gases  (Compressors) 
Riveting  and  Calking  Tanks 
Calking  and  Testing   Pipe   Linen 
Vaporizing    Oil    for    Oil    Engines 
High  Pressure  Gas  Transmission 

(Compressors) 

GLASS  WORKS 
Pumping  Glass  Sand  by  the  Re- 
turn Air  System 
Blowing  Glass 

Operating    Molds    and    Presses 
Supplying  Oil  Burners 
Operating  Sand  Blasts 
Etching  Glass 

GRAIN  ELEVATORS 
Drying  Grain 

HAT  FACTORIES 
Operating  Presses 
Cleaning  the   Machines  with  the 
Air  Jet 

ICE    AND    REFRIGERATING 
PLANTS 

Pumping  and  Aerating  Water 
Air  Hoists  for  Ice  Tanks 
Air  Hoist  for  Loading  Cars 
Scaling  Condenser  Coils 
Cleaning  Boiler  Flues 

IRRIGATION 

Pumping  Water  by  the  Air  Lift 
or  Displacement   Systems 

JUTE  MILLS 
Pumping  Water 

Operating  Air  Hoists,   Lifts   and 
Motors 

KNITTING  MILLS 

Pumping  Water 
Cleaning  with  the  Air  Jet 
Agitating,   Elevating  and  Trans- 
ferring Solutions 
Automatic  Sprinkler  System 
Air  Hoists,  Lifts  and  Motors 

MACHINE  SHOPS 

Pumping  Water 

Operating  Pneumatic  Hammers 

and  Drills 
Supplying   Power  Hammers,   Air 

Hoists,  Lifts  and  Jacks 
Air  Motors  for  Grinding,  Buffing, 

etc. 


Sand  Blasts  for  Cleaning  Metals 
Cleaning  Machines  with  the  Air 

Jet 
Belt  Shifters  for  Heavy  Machine 

Tools 

Punches  and  Presses 
Pipe  Bending  Machines 

MINING 

Running  Rock  Drills  and  Ham- 
mer Drills 

Return-Air  System  for  Station 
and  Sump  Pumping 

Unwatering    by    the    Air    Lift 
System 

Air  Hoists  and  Motors 

Pneumatic  Tools  for  the  Repair 
Shop 

Operating  Air  Brakes  on  Hoists 

Unloading  Cars 

Running    Direct-Acting    Pumps 

Drill  Steel  Sharpeners 

Blowing  Smith  Fires 

Oil  Furnaces  for  Steel  Sharpeners 

Pile  Drivers  for  Shaft  Work 

MUNICIPALITIES  AND  PUB- 
LIC INSTITUTIONS 

Pumping  Water  by  the  Air  Lift 
or  Return-Air  System 

Pumping  Sewage 

Testing  and  Calking  Pipe  Lines 

Rock  Drills  in  Road  Construction 

Blowing  Fire  Whistles 

Filtration  Plants 

OFFICE    BUILDINGS    AND 

HOTELS 

Sewage  and  Drainage  Ejectors 
Pneumatic  Clocks 
Operating  Elevator  Doors 
Cleaning  with  the  Air  Jet 
Dentist,    Physician    and    Barber 

Service 
Accumulator  Systems 

OIL  REFINERIES 
Displacing   and   Transferring   Oil 
Agitating  and  Transferring  Acids 
Pneumatic   Hammers   and    Drills 
Calking  Tanks  and  Pipe  Lines 
Air  Hoists  and  Lifts 
Oil  Wells 

Pumping  by  the  Air  Lift  or  Dis- 
placement Systems 

PACKING  HOUSE  PLANTS 

Pumping  Water 
Stuffing  Sausages 
Operating  Belly  Pounders 


AND 

CONDENSERS 

FOR 

EVERY" 

5 

ERVICE 

4 

49 


c 

u 

N 

IO 

N 

STE 

AM 

P 

UM 

P 

CO 

M  P  AN  Y     ll| 

Lard  Refineries 

Air  Hoists,  Lifts  and  Motors 

PAINT  FACTORIES 
Dressing  Burr  Stones 
Agitating  and  Transferring  Mix- 
tures 
Air  Hoists  and  Lifts 

PRINTING  SHOPS 

Monotype  Machines 
Air  Hoists  and  Lifts 
Cleaning  by  the  Air  Jet 

QUARRIES 

Rock  Drills,  Hammer  Drills  and 

Plug  Drills 
Stone  Channelers 
Air  Hoists,  Lifts  and  Motors 
Drainage  Pumping  by  the  Return 

Air  System 

Operating  Direct-Acting  Pumps 
Splitting  Stone  in  the  Bed 

RAILROADS 

Starting  Fires  in  Locomotives 
Operating    Pneumatic    Hammers 

and  Drills 
Cleaning  Flues 
Calking  Boilers  and  Tanks 
Air  Hoists,  Lifts  and  Jacks 
Air  Brakes 
Turn-Table  Motors 
Crossing  Gates 
Switch  and  Signal  Systems 
Sand  Blast  for  Removing  Paint, 

Cleaning  Castings,  etc 
Pneumatic  Sand  Rammers 
Paint  and  Whitewash  Spraying 
Cleaning   Cars,    Furnishings,    etc. 
Transferring  Oil 
Pumping  Water 
Track  Sander 
Valve  Setting  Machines 

ROAD  BUILDING 

Running   Rock    Drills    and    Plug 
Drills 

RUBBER  FACTORIES 

Testing  Rubber 

Inflating  Rubber  Tires 

Testing  Tires,  etc. 

Air  Hoists,  Lifts  and  Motors 

SALT  MINES 

Rock  Drills  and  Plug  Drills 

SALT  WELLS 
Pumping  Brine 


SAND  PITS 

Pumping  Sand  by  the  Return-Air 
System 

SAW  MILLS 

Operating     Edgers,     Bumpers, 

Pickups,  etc. 
Blowing    Sawdust    and    Shavings 

from  Machines 
Pneumatic   Haulage 
Pumping  Water 
Automatic  Sprinkler  System 

SEWAGE  AND  TRENCH 

WORK 

Rock  Drills  and  Hammer  Drills 
Sheet  Pile  Drivers 
Calking  and  Testing  Pipe  Lines 

SHIPYARDS  AND  BOAT 

BUILDERS 

Pneumatic   Hammers   and    Dril's 
Air  Hoists,  Lifts  and  Motors 
Cleaning  Plates  and  Castings  by 

the  Sand  Blast 
Pneumatic  Painting 
Starting  Gasoline  Engines 
Riveting  and  Calking 

SMELTERS  AND  ORE  MILLS 

Converter    Tamping    Machines 
Air  Hoists  and  Lifts 
Blowing  Converters 
Agitating  Cyanide  Solution 
Cleaning  Cyanide  Tanks  by  the 

Sand  Blast 
Calking  Tanks 
Handling  Solutions 

STEAM  POWER  PLANTS 
Cleaning  Boiler  Flues 
Calking  Boilers 
Pumping  Water 
Air  Hoists  and  Lifts 

STORE  SERVICE 
Pneumatic  Cash  Carriers 
Cleaning  by  the  Air  Jet 

STRUCTURAL  WORKS 
Pneumatic   Tools   for   Drilling, 

Reaming,     Chipping,     Scaling, 

Riveting  and  Calking 
Air  Hoists 
Pneumatic  Punches 
Rock  Drills  and  Plug  Drills 
Drainage  Pumps 

SUGAR  REFINERIES 
Agitating  and  Transferring  Syrups 


50 


Pumping  Water 
Air  Hoists  and  Lifts 
Pressure  Filters 

TANNERIES 
Pumping  Water 
Handling  Tan  Liquid 
Air  Hoists  and  Lifts 

THEATRES  AND  HALLS 

Cleaning  with  the  Air  Jet 
Displacing  Water 
Handling   Scenery   with   the   Air 
Hoist  and  Lift 

U.  S.  GOVERNMENT 
Pneumatic  Tube  Systems 
Torpedo  Chargings 
Ammunition  Hoists 
Pumping  Water 
Sand  Blasts 

WAREHOUSES     AND 
STORAGE 

Air  Hoists  and  Lifts 
Air  Motors 
Air  Cleaning 


WATCH  FACTORIES 

Blowing   Dust,   Chips,   etc.,   with 

the  Air  Jet 
Pneumatic  Tools 
Air  Hoists  and  Motors 

WATER  WORKS 
Pumping  Water 
Cleaning  Boiler  Flues 
Calking  Boilers  and  Tanks 
Calking  and  Testing  Pipe  Lines 
Sheet  Pile  Drivers 
Plug  Drills  and  Rock  Drills  for 
Trenching 

WOODWORKING  MILLS 
Bending  Wood 

WOOLEN  MILLS 

Pumping  Water 

Agitating  and  Handling  Dyes  and 

Solutions 
Cleaning    Looms,    Doffers    and 

Spindles 

Air  Motors,  Hoists  and  Lifts 
Pressure  Accumulators 
Starting  Gas  and  GasolineEngines 


AND    CONDENSERS    FOR    EVERY  SERVICE 


51 


Compressor  Data  Required  for   Full   and 
Correct  Reply 

When  writing  for  information  or  prices  on  compressors,  you 
will  insure  a  prompt,  full  and  satisfactory  reply  by  giving  us  as 
far  as  possible  answers  to  the  following  questions: 
Method  of  Drive  — If  Steam. 

1.  Maximum    and    minimum    pressure    at    compressor 
throttle,  or 

2.  Boiler  pressure,  distance  from  boiler  to  compressor, 
and  size  of  steam  pipe? 

3.  To  operate  condensing  or  non-condensing? 

4.  Are  we  to  furnish  condenser? 

5.  Have  you  any  preference  as  to  type  of  engine  or  steam 
valve  to  be  used?     Refer  to  cut  in  catalogue  or  advise  in  detail. 

6.  Special  features  or  remarks  ? 
If  Electric. 

7.  Voltage  of  motor? 

8.  Direct  current  or  alternating? 

9.  If  alternating,  phases  and  cycles? 

10.  Gear,  chain  or  belt  drive? 

11.  Slow,  moderate  or  high-speed  motor? 

12.  Have  you  any  preference  as  to  type  or  make  of  motor? 

13.  Special  features  or  remarks  ? 
Volume  of  Air  Required. 

14.  Maximum  air,  cubic  feet  per  minute? 
Free  or  compressed  air?     State  which. 

15.  Maximum  gauge  pressure  at  machine,  or 

16.  Maximum  gauge  pressure  at  work? 

17.  Distance  from  compressor  to  work? 

18.  Character  of  work  to  be  done? 

19.  Altitude   above   sea  level  where   compressor  will   be 
located? 

20.  Special  features  or  remarks  ? 
General  Conditions. 

21.  Floor  space  and  head  room,  if  limited? 

22.  Are  we  to  install? 

23.  Character  of  work  for  which  required,   such   as  gas 
compression,  air  lift  pumping,  handling  oil  or  acids,  etc.? 

24.  Approximate  hours  per  day  compressor  will  operate? 

25.  Comments  and   remarks? 


52 


Cost  of  Compressing  Air 
Coal,  Gasoline,  and  Electric  Current  Compared 

In  the  contemplation  of  purchasing  a  relatively  small  air 
compressor  unit,  say  30  to  100  H.  P.  capacity,  it  is  often  de- 
sirable to  consider  various  sources,  of  power  for  operating  it 
and  the  cost  of  fuel.  Data  given  in  the  Practical  Reference 
Tables  have  been  compiled  to  show  readily  these  comparisons 
wherein  the  air  compressor  is  to  be  driven  either  by: 

1.  Steam  Engine,  direct  connected  or  belt  driven. 

2.  Gasoline  Engine,  direct  connected  or  belt  driven. 

3.  Electric  motor,  direct  connected  or  belt  driven. 

It  may  be  noted  from  the  example  given  in  each  table  that 
to  compress  and  deliver  100  cu.  ft.  of  free  air  at  90  Ib.  pressure, 

1.  The  cost  of  coal  will  be  0.5232  cent 

2.  The  cost  of  gasoline  will  be  1 .08       cents 

3.  The  cost  of  electric  current  will  be    1.1         cents 
when  the  cost  of  coal  is  taken  at  $6.00  per  ton,  gasoline  at  22 
cents  per  gallon,  and  electric  current  furnished  by  a  steam  oper- 
ated commercial  distributing  plant  at  4  cents  per  K.  W.  Hour. 

In  using  these  tables,  it  is,  of  course,  necessary  to  assume 
certain  figures  suiting  local  conditions  in  order  to  make  proper 
comparisons,  after  first  determining  the  horsepower  required 
to  compress  and  deliver  100  cu.  ft.  of  free  air  per  minute  and 
assuming  the  mechanical  efficiency  of  all  the  machines  is  about 
the  same. 

In  Table  I,  the  steam  consumption  of  the  engine  must  be 
approximately  determined.  In  the  example,  it  is  taken  at 
34  Ibs.  per  horsepower  per  hour;  if  it  were  17  Ibs.,  the  cost  of 
coal  would  be  one-half.  The  boiler  evaporation  in  the  table 
is  given  as  delivering  to  the  engine  7  Ibs.  of  water  for  each 
pound  of  coal  burned,  and  any  percentage  of  variation  from 
this  performance  should  appear  in  the  calculations.  When 
the  final  figure  of  cost  in  the  table  is  determined,  it  must  be 
multiplied  by  the  cost  of  coal  in  dollars  per  ton.  A  steam 
driven  compressor  requires  boiler  power,  and  the  cost  of  this 
and  the  expense  of  operating  it  must  be  considered,  when 
comparing  with  other  sources  of  power,  aside  from  the  cost  o: 
coal  which  latter  is  covered  by  the  table. 

In  Table  II,  the  gasoline  consumption  per  brake  horse- 
power will  not  vary  greatly,  but  the  percentage  of  variation 
should  be  considered.  If  kerosene  or  other  oils  are  burned 


.AND    CONDENSE RS    F O R   E VE RV  SE RVI C  E 


[l 

u 

N 

1  O 

N 

S 

TEAM 

P 

UM 

P 

COMPANY 

J 

instead  of  gasoline,  the  price  per  gallon  should  be  determined, 
also  the  consumption  per  brake  horsepower. 

In  Table  III,  it  is  assumed  that  the  consumer  may  wish  to 
buy  electric  current  from  some  power  plant. 

The  figures  in  all  the  tables  are  given  in  multiples  so  that 
missing  ones  can  readily  be  determined;  for  illustration,  if 
100  cu.  ft.  of  free  air  requires  10  H.  P.,  one  half  the  horizontal 
column  of  30  or  one-third  of  30  can  be  taken.  If  gasoline  costs 
20  cents,  multiply  by  2  the  column  given  u'nder  10  cents.  If 
electric  current  costs  6  cents,  multiply  by  2  the  column  given 
under  6  cents. 

These  tables  can  be  used  to  advantage  in  considering  a 
plant  of  any  size  or  efficiency. 

Note — In  the  cost  figures  the  element  of  time  need  not  be  considered  in  compressing 
100  cu.  ft.  of  air,  whether  it  icquires  one-quarter  minute,  one-half,  etc.,  to  do  the  work. 

TABLE  I 

Cost  of  Coal  at  One  Dollar  Per  Ton  to  Compress 
and  Deliver  100  Cubic  Feet  of  Free  Air 

(Multiply  figures  in  table  by  price  of  coal  in  dollars  per  ton.     Ton  equals  2000  pounds). 
Weight  of  Steam — in  Pounds — Required  by  the  Engine — Per  Horsepower  per  Hour. 


24 


26 


28 


30 


32 


34          36          38 


40        42 


Weight  of  Coal — in  Pounds — Per  Horsepower  per  Hour — WhenBoiler  is  Evaporating  7  pound, 
of  Water  per  Pound  of  Coal. 

3.43      3.714      4.        4.286   4.571    4.757    5.143    5.428    5.714       6 


Cost  of  Coal  per  Horsepower  at  One  Dollar  per  Ton — Fractions  of  Cent. 


Brake  H.  P 

deliver  100  c 
free  air  per  n 

.1715 

.1857 

2 

.2143 

.2285 

.2378 

.2571 

.2714 

.2857 

.3 

Cost  of  Coal  per  100  Cubic  Feet  Free-Air—  Fractions  of  Cent. 

16 

.0457 

.0495 

.0533 

.0572 

.0610 

.0634 

.0686 

.0724 

.0762 

.08 

18 

.0514 

.0557 

.06 

.0643 

.0686 

.0714 

.0772 

.0814 

.0857 

.09 

20 

.057 

.0619 

.0667 

.0714 

.0762 

.0793 

.0857 

.0904 

.0952 

.10 

22 

24 
26 

.0627 

.0681 

.0733 

.0785 

.0838 

.0872 

.0943 

.0995 

.1047 

.11 

.0684 

.0743 

.08 

.0857 

.0914 

.0951 

.1029 

.1085 

.1142 

.12 

.0741 

.0805 

.0866 

.0929 

.099 

.103 

.1114 

.1175 

.1238 

.13 

28 

.0798 

.0^67 

.0933 

.10 

.1066 

.1109 

.12 

.1266 

.1334 

.14 

30 

.0855 

.0929 

.10 

.1071 

.1142 

.1189 

.1285 

.1357 

.1429 

.15 

Example — If  it  requires  22  brake  horsepower  to  deliver  100  cubic  feet 
of  free  air  per  minute  at  90  pounds  pressure,  and  the  compressor  is  driven 
by  an  ordinary  steam  engine  requiring  34  pounds  of  steam  per  horse- 
power hour,  and  an  ordinary  boiler  evaporating  7  pounds  of  water  per 
pound  of  coal,  and  with  coal  at  $6  a  ton — the  coal  cost  per  100  cubic 
feet  of  free  air  is  .0872x6=. 5232  cent. 


54 




BATTLE      CREEK.     MICHIGAN,      U.S.A. 


TABLE  II 

Cost  of  Gasoline  in  Cents  to  Compress  and 
Deliver  100  Cubic  Feet  of  Free  Air 

Gasoline  Consumption  One  Pint  Per  Brake  Horsepower  Per  Hour 


Brake  H.  P.  to 
deliver  100  Cu. 


Price  of  Gasoline  per  Gallon 
Qents 


Ft.  Free  Air 
per  Minute 

8 

9 

10 

11 

12 

13 

14 

15 

16 

.266 

.300 

.333 

.366 

.400 

.433 

.465 

.500 

18 

.300 

.337 

.375 

.413 

.450 

.487 

.525 

.562 

20 

.333 

.375 

.416 

.458 

.500 

.542 

.584 

.626 

22 

.366 

.412 

.458 

.504 

.550 

.595 

.642 

.687 

24 

.400 

.450 

.500 

.550 

.600 

.650 

.700 

.750 

26 

.433 

.488 

.542 

.596 

.650 

.705 

.759 

.813 

28 

.466 

.525 

.583 

.642 

.700 

.758 

.816 

.875 

30 

.500 

.563 

.625 

.688 

.750 

.813 

.875 

.938 

Example — If  it  requires  22  Brake  Horsepower  to  deliver  100  cubic 
feet  of  free  air  per  minute  at  90  pounds  pressure,  and  gasoline  at  22  cents 
per  gallon,  the  gasoline  cost  per  100  cubic  feet  of  free  air  is  .504x2=1 .08 
cents. 

TABLE  III 

Cost  of  Electric  Current  in  Cents  to  Compress 
and  Deliver  100  Cubic  Feet  of  Free  Air 


Price  of  Electric  Current  per  Kilowatt-Hour — Cents 


<^s<% 

«78§ 
||£s 

ll£l 

1. 

1.5 

2. 

2.5 

3. 

3.5 

4. 

4.5 

5. 

Per  Horsepower  Hour  —  Cents 

.75 

1.125 

1.5 

1.875 

2.25 

2.625 

3. 

3.375 

3.75 

16 

.2 

.3 

.4 

.5 

.6 

.7 

.8 

.9 

1.0 

18 

.225 

.337 

.45 

.562 

.675 

.787 

.9 

1.012 

1.125 

20 

.25 

.375 

.5 

.625 

.687 

.75 

.875 
.962 

1.0 

1.125 

1.25 

22 

.275 

.412 

.55 

.825 

1.1 

1.237 

1.375 

24 

.3 

.45 

.6 

.75 
.812 

.9 
.975 

1.05 
1.137 
1.225 

1.2 
1.3 

1.35 

1.5 

26 

.325 

.487 

.65 

1.46 

1.625 

28 

.35 

.525 

.7 

.875 

1.05 

1.4 

1.575 

1.75 

30 

.375 

.562 

.75 

.937 

1.125 

1.312 

1.5 

1.687 

1.875 

Example — If  it  requires  22  Brake  Horsepower  to  deliver  100  cubic 
feet  of  free  air  per  minute  at  90  pounds  pressure,  and  electric  current  at 
4  cents  per  kilowatt-hour,'  the  electric  current  cost  per  100  cubic  feet  of 
free  air  is  1.1  cents  -  H.  V.  CONRAD. 


r 

AND 

CONDENSERS 

FOR 

EVERT 

SERVICE      ^ 

55 


UNION       S  T  E  AM       P  U  M  P       COMPANY 


1 


if 
I 


PUMPING  MACHINERY;  AIR  COMPRESSJDRS 


5G 


Pumping  with    Compressed  Air 

The  air  lift  pumping  system  is  a  method  of  lifting  water  or 
other  fluid  by  means  of  compressed  air.  This  method  of  pump- 
ing is  generally  employed  where  conditions  are  such  that  it  is 
impractical  to  use  a^mechanical  pump. 

Advantages 

The  principal  advantages  of  the  air  lift  system  of  pumping 
are  the  following: 

Quantity:  There  is  no  question  but  that  more  water  can 
be  secured  from  a  deep  well  with  the  air  lift,  than  by  any  other 
method  06  pumping,  providing  the  conditions  are  suitable  for 
its  use. 

Quality:  The  aeration  of  the  water  produced  by  the  air 
lift  system  of  pumping  is  acknowledged  to  be  one  of  the  prin- 
cipal methods  for  purifying  water  in  nitration  plants. 

If>  free  sulphur  gas  is  encountered  in  the  well,  it  is  almost 
completely  removed  by  the  action  of  the  aeration  in  the  air  lift. 

Temperature:  With  the  air  lift  system  of  pumping,  the 
expansion  of  the  air  lowers  the  temperature  of  the  water. 

Simplicity :  The  air  lift  is  the  simplest  method  of  pumping, 
and  it  requires  the  least  attention  and  repairs.  With  the  air 
lift  all  the  machinery  is  in  the  power  house,  and  all  trouble  such 
as  pulling  sucker  rods,  working  barrels,  etc.  is  eliminated. 

Terms  Used  in  Air  Lift  Work 

In  discussing  the  air  lift  and  air  lift  propositions,  certain 
general  terms  are  used  that  must  be  understood.  By  referring 
to  figure  38,  page  58,  these  terms  are  explained  thusly : 

Static  Head:  Normal  water  level^  when  not  pumping, 
measured  from  the  surface  or  ground  level. 

Drop :  Point  to  which  the  water  level  drops  below  the 
static  head,  while  being  pumped. 

Pumping  Head :  Level  of  water  when  pumping,  with  reference 
to  the  ground  level.  Pumping  head  equals  static  head  plus  the 
drop. 

Elevation:  Point  above  ground  level  to  which  the  water 
is  raised. 

Total  Lift:  The  distance  water  is  raised,  from  level,  when 
pumping,  to  point  of  discharge.  Total  Lift  equals  elevation 
plus  static  head  plus  drop. 


57 


UNION       STEAM       PUMP       COMPANY 


Fig.  38. 
Diagram  of  an  Air  Lift. 


Submergence:  The  distance  below  the  pumping  head  at 
which  the  air  picks  up  the  water. 

Starting  Submergence:  The  distance  below  the  static  head 
at  which  the  air  picks  up  the  water.  Starting  submergence 
equals  drop  plus  submergence. 

Ratio  of  Submergence 

If  you  have  a  given  ascertained  percentage  of  submergence, 
the  actual  submergence  would  be  ascertained  by  multiplying 
the  lift  by  the  percentage  of  submergence,  and  dividing  the  pro- 
duct by  one  hundred  minus  the  percentage  of  submergence,  as 
expressed  in  the  following  equation  : 

Submergence  =Hft  X  Percentage  of  ^mergence.  (W) 

100  —  percentage  of  submergence. 

The  percentage  or  the  ratio  of  submergence  is  expressed 
as  follows: 


Ratio  =  -  •  •  (20) 

lift  4-  submergence. 

The  necessary  percentage  of  submergence  varies  with  the 
lift;  low  lifts  require  proportionately  more  submergence  than 
high  lifts. 

The  following  gives  an  idea  of  the  proportion  of  submergence 
to  lift,  for  good  results: 

For  lifts  up  to    50  feet  66%  submergence. 

"      "        "        50  to  100  ft.  60%  submergence 

"      "        "      100  to  200  ft.  55%  submergence 

"      "        "      200  to  500  ft.  50%  submergence. 

"      "        "      300  to  400  ft.  45%  submergence. 

"      "        "      400  to  500  ft.  40%  submergence. 

The  Air  Lift  Installation 

To  secure  the  best  results,  compressed  air  should  be  in- 
troduced into  the  well  in  a  finely  divided  state,  so  that  the 
bubbles  are  small  and  equally  distributed  throughout  the  water. 
It  is  evident  that  if  the  air  pipe  merely  discharges  the  air  into 
the  water  through  a  full  opening  in  the  pipe,  the  result  will  be 
large  bubbles  instead  of  the  equally  divided  condition  which  is  de- 
sired. It  is  therefore  advisable  to  either  cap  the  end  of  the  air 


59 


UNION       STEAM       PUMP       COMPANY 


pipe  and  drill  small  holes  in  the  side  near  the  end,  or  use  an  air 
nozzle  as  shown  in  figure  38,  so  that  the  air  will  be  admitted  to 
the  water  in  small  jets  which  will  produce  the  small  bubbles 
necessary  for  efficient  results. 

Inasmuch  as  the  action  of  the  air  lift  depends  upon  form- 
ing an  emulsion  of  air  and  water,  which  is  lighter  than  water, 
it  is  evident  that  a  perfect  condition  would  be  one  in  which  the 
bubbles,  when  introduced  in  the  bottom  of  the  well,  would 
maintain  the  same  size  in  their  passage  to  the  discharge.  It 
will  be  readily  seen,  however,  that  inasmuch  as  the  pressure 
is  relieved  from  the  air  bubbles  as  they  rise  toward  the  surface, 
the  bubbles  become  larger  and  larger;  the  proportion  of  the 
air  to  the  water  increases  exactly  in  proportion  to  the  expan- 
sion, and  this  decreases  the  efficiency  of  the  lift. 

This  expansion  of  air,  because  it  requires  an  increased 
volume  per  minute  to  pass  through  the  pipe,  has  the  effect  of 
throttling  the  mixture  of  air  and  water,  which  is  another  source 
of  loss  in  efficiency.  The  ideal  lift  would  have  its  discharge 
line  so  proportioned  that  its  area  would  be  constantly  increased. 
The  proportion  to  this  increase  in  volume  thus  keeps  the  ve- 
locity constant.  In  deep  wells,  it  is  advisable  to  approximate 
this  condition  by  installing  the  discharge  line  in  sections  of 
different  diameters. 

Air  and  Water  Pipes 

The  following  table  gives  the  sizes  of  water  and  air  pipes 
required  for  the  central  pipe  system  of  pumping  as  illustrated 
on  page  58.  The  size  of  well  casing  and  the  pumping  capacity 
for  which  these  pipes  are  adapted  is  also  given.  The  drop  pipe 
should  extend  below  the  air  nozzle  not  less  than  5  feet,  and  from 
15  to  20  feet,  if  possible,  depending  upon  the  depth  of  the  well. 


Smallest  Well 
Casing 

Water 
Pipe 

Central 
Air  Pipe 

Capacity,  Gallons 
Per  Minute 

2^ 

IK 

y* 

10-20 

3  2 

2 

% 

20-40 

2H 

i 

40-60 

4^ 

3 

IK 

60-80 

5* 

3  ^ 

80-100 

6 

4 

i  ^ 

100-150 

7 

5 

2 

150-250 

g 

6 

2 

275-375 

10 

8 

2V£ 

500-650 

12 

10 

2^ 

775-1000 

Calculation  of  the  Air  Lift. 

We  are  now  prepared  to  consider  a  concrete  prob- 
lem in  air  lift  pumping.  Given  a  well  with  a  7  inch  casing, 
300  feet  deep,  the  water  in  which  stands  75  feet  below  the  ground 
level,  but  which  falls  10  feet  when  being  pumped  at  the  rate  of 
200  gallons  per  minute,  and  it  is  required  to  raise  the  water  15 
feet  above  the  ground. 

Then  from  the  above* 

Static  Head  equals 75  feet 

Drop  equals 10  feet. 

Pumping  head  equals 85  feet. 

Elevation  equals.' 15  feet. 

Total  lift  equals 100  feet. 

By  referring  to  the  table  on  page  59,  the  percentage  of  sub- 
mergence for  100  feet  lift  is  60%.  Substituting  this  value  in 
equation  19,  on  page  59, 

100  X  60      6000 

=  150  ieet  submergence. 


100  -  60        40 

With  150  feet  submergence,  and  with  the  pumping  head 
given  of  85  feet,  the  distance  from  the  surface  of  the  ground 
to  the  bottom  of  the  air  pipe  or  nozzle  will  be, 

150  +  85  =  235  feet. 

As  stated  on  page  63,  the  drop  pipe  should  (if  possible), 
extend  down  15  to  20  feet  below  the  air  pipe,  or  in  the  example 
given,  255  feet  from  the  surface  of  the  ground. 

Referring  to  table  on  page  63,  the  compressor  displacement 
required  to  elevate  200  gallons  per  minute  against  a  total  lift  of 
100  feet  with  60%  submergence  is: 

200  X   .585  =  117.0  cubic  feet  of  free  air  per  minute. 


AND    CONDENSERS    FOR    EVERY  SERVICE 


|[        UNION 

STEAM 

P  UM  P 

COM  P  ANY 

J 

The  indicated  or  brake  horse  power  required  to  operate 
the  compressor  having  117  cubic  feet  displacement  may  be 
calculated  by  referring  to  the  table  for  single  stage  compression, 
on  page  38.  The  horse  power  per  cubic  foot  displacement  at 
67J  pounds  working  pressure  (interpolating  between  65  pounds 
'and  70  pounds)  is  .147  and 

.147  X  117  =  17.19  Ind.  or  B.  H.  P. 
required  to  operate  the  compressor. 

The  next  calculation  is  to  find  the  starting  and  working 
pressures.  The  pumping  head  is  10  feet  greater  than  the  static 
head,  which  indicates  a  starting  submergence  of  150  +  10  =  160 
feet. 

Starting  pressure  equals: 

Starting  submergence  X  .45 
Working  pressure  equals: 

Submergence   X   .45 

Substituting  the  values  of  the  above  example, 
,  The  starting  pressure  equals : 

160  X   .45  =  72  pounds. 
Working  pressure  equals 

150  X  .45  =  67X  pounds. 

In  the  table  on  page  63,  the  working  pressure  is  given,  and 
the  starting  pressure  may  be  calculated  as  above. 

Then,  referring  to  the  table  on  page  60,  for  the  conditions 
given  in  the  example,  it  will  require  a  5-inch  drop  pipe,  and  a 
2-inch  air  pipe. 

In  calculating  an  air  lift,  the  pumping  head  in  a  well  can 
seldom  be  known  in  advance  of  a  test.  It  is  customary  to  assume 
certain  conditions  of  lift  and  submergence  based  on  experience, 
and  pipe  the  well  accordingly.  After  the  pipe  is  installed,  the 
submergence  is  altered  to  suit,  by  raising  or  lowering  the  pipe 
in  the  well  until  the  best  results  are  obtained. 


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AND    CONDENSERS    FOR   EVERV  SERVICE 


63 


Information  Required  for  Correct  Recommenda- 
tion for  Air-Lift  Pumping 

Air  Lift  Pumping. 

Number  of  wells  and  relative  locations,  distance  apart  and 
distance  from  proposed  location  of  compressor.  Also  the 
following  for  each : 

1.  Entire  depth  of  well. 

2.  Inside  diameter. 

3.  If  boring  is  reduced,  state  at  what  depth  and  to  what 
diameter. 

4.  If  cased,  state  inside  diameter  of  casing. 

5.  Depth  from  surface  to  water  level  when  not  pumping. 

6.  Capacity  of  well  at  present  when  pumped  in  gallons 
per  minute. 

7.  Depth  from  surface  to  water  level  when  pumped  at 
this  capacity. 

8.  Style,  kind,  size,  and  capacity  of  pump  at  present  used. 

9.  Elevation  above  ground  surface  to  which  water  is  to 
be  raised. 

10.  Horizontal  distance  from  well  to  tank. 

11.  Is  compressor  to  be  operated  by  steam  direct,  electric 
motor  or  belt  power? 

12.  If  by  steam  direct,  state  steam  pressure  carried. 

13.  At  what  depth  below  the  surface  is  the  source  of  water 
located  ? 

14.  Number  of  gallons  per  minute  required. 


BATTLE      CREEK.     MICHIGAN,     U.S.A. 


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AND    CONDENSERS    FOR    EVERV  SERVICE 


Horse- Power,  Efficiency  and   Terminal  Temper- 
ature in  Air  Compression  to  Various 
Pressures 

Single  and  Two  Stage  Compression 


Isother- 
mal 
Com- 
pression 

Single  Stage 
Adiabatic 
Compression 

Two  Stage 
Compression 

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462 

800 

55  4 

.258 

.488 

.52 

1208 

.373 

.69 

468 

850 

58.8 

.262 

.50*0 

.52 

1237 

.381 

.69 

480 

900 
950 

62.2 
65.6 

.265 
.268 

.512 
.523 

.52 
.51 

1265 
1292 

388 
.395 

.68 
.68 

490 

495 

1000 

69. 

.272 

.534 

.51 

1318 

.403 

.67 

498 

1100 
1200 

75.8 
82.6 

.278 
.283 

.555 
.575 

.50 
.49 

1367 

1415 

.416 
.429 

.67 
.66 

507 
525 

1300 
1400 

89.4 
96.2 

.289 
.293 

.594 
.611 

.49 

.48 

1457 
1498 

.441 
.452 

.66 
.65 

534 
550 

1500 
1600 

103. 
109.8 

.297 
.301 

.627 
.643 

.48 

.47 

1537 
1575 

.462 

.472 

65 
.64 

563 
568 

1700 

116.6 

.305 

.659 

.47 

1610 

.482 

.63 

589 

1800 

123.4 

.309 

.673 

.46 

1645 

.491 

.63 

606 

1900 
2000 

130.2 
139. 

.313 
.317 

.687 
.701 

46 
.45 

1678 
1709 

.500 
.509 

.63 
.62 

628 
639 

2250 

154. 

.324 

.733 

.44 

1784 

528 

.62 

645 

2500 

171. 

.331 

.763 

.43 

1852 

.547 

.61 

654 

3000 

205. 

.342 

.816 

42 

1975 

.579 

.59 

670 

PUMPING    M  AC  H  INJURY.    AIR   c'OMPR  ESS  OJtS 


••  ft  »  w  »  v 


n 

ATT 

LE 

C 

REE 

K. 

MICH 

IG 

AN, 

U. 

S. 

A.        | 

Horse-Power,  Efficiency  and   Terminal   Temper- 
ature in  Air  Compression  to  Various 
Pressures 

Three  and  Four  Stage  Compression 


Isother- 
mal Com- 
pression 

Three  Stage 
Compression 

Four  Stage 
Compression 

a 

c 

I 

y 

ttl 

'8   si 

5     o£ 

4i 

el 

6 

5     "o  o. 

tj 
1 

OH 
* 

i 

tmospheres 

.  P.  required 
>mpress  One 
sot  per  Minu 

.  P.  required 
)mpress  One 
)ot  Free  Air 
Inute 

ftciency  as  c( 
.red  to  Isothe 

nal  Tempera 
jgrees  Fahr. 
srfect  Intercc 
liabatic  Com 

.  P.  required 
>mpress  One 
>ot  Free  Air 
inute 

ficiency  as  cc 
red  to  Isothe 

nal  Temperai 
igrees  Fahr. 
irfect  Interco 
liabatic  Com 

o 

< 

Wofe 

Wo£s 

W  a 

feQCL,*} 

WcjfcS 

W  o, 

fePa,< 

5 

1.34 

.0188 

10 

1.68 

.0333 

15 

2.02 

.0481 

20 

2.36 

.0551 

25 

2.70 

.0638 

30 

3.04 

.0713 

40 

3.72 

.0843 

50 

4.40 

.0948 

60 

5.08 

.1037 

70 

5.76 

.1120 

80 

6.44 

.1196 

90 

7.12 

.1260 

100 

7.80 

.1320 

110 

8.48 

.1371 

120 

9.16 

.1422 

130 

9.84 

.1467 

140 

10.52 

.1510 

150 

11.20 

.1547 

.182 

.85 

200 

160 

11  .88 

.1583 

.187 

.85 

204 

180 

13.24 

.1656 

.197 

.84 

211 

200 

14.60 

.1720 

.206 

.83 

218 

225 

16.3 

.1790 

.215 

.83 

224 

250 

18. 

.1860 

.224 

.83 

230 

275 

19.7 

.1-920 

.233 

.82 

236 

300 

21  A 

.1970 

.241 

.82 

241 

350 

24.8 

.2060 

.252 

.82 

250 

400 

28.2 

.2140 

.262 

.82 

258 

450 

31.6 

.2230 

.272 

.82 

266 

500 

35. 

.2290 

.282 

.81 

275 

26. 

.88 

215 

550 

38.4 

.2340 

.292 

.80 

283 

26.9 

.87 

220 

600 

41.8 

.240 

.300 

.80 

290 

27.8 

.86 

225 

650 

45.2 

.245 

.310 

.79 

295 

28.4 

.86 

228 

700 

48.6 

.249 

.320 

.78 

300 

29. 

.86 

234 

750 

52. 

.252 

.327 

.78 

305 

29.6 

.85 

236 

800 

55.4 

.258 

.334 

.78 

309 

30.2 

.85 

240 

850 

58.8 

.262 

.341 

.77 

314 

30.7 

.85 

244 

900 

62.2 

.265 

.347- 

.76 

319 

31  .,2 

.85 

247 

950 

65.6 

.268 

.354 

.76 

322 

31.6 

.85 

250 

1000 

69. 

.272 

.360 

.75 

325 

32. 

.85 

252 

1100 

75.8 

.278 

.370 

.75 

331 

32.7 

.85 

254 

1200 

82.6 

.283 

.381 

.74 

338 

33.4 

.84 

258 

1300 

89.4 

.289 

.390 

.74 

342 

34.1 

.84 

265 

1400 

96.2 

.293 

.399 

74 

349 

34.8 

.84 

270 

1500 

103. 

.297 

.406 

73 

353 

35.5 

.84 

273 

1600 

109.8 

.301 

.415 

.73 

358 

36.1 

.83 

276 

1700 

116.6 

.305 

.424 

.72 

364 

36.7 

.83 

280 

1800 

123.4 

.309 

.431 

.72 

370 

37   2 

.83 

284 

1900 

130.2 

.313 

.438 

.72 

374 

37.7 

.83 

287 

2000 

139. 

.317 

.444 

.71 

378 

38.1 

.83 

290 

2250 

154. 

.324 

.460 

.70 

385 

39.3 

.82 

294 

2500 

171. 

.313 

.474 

.70 

398 

40.5 

.82 

298 

3000 

205. 

.342 

.500 

.69 

414 

42. 

.81 

308 

AND    CONDENSERS.   FOR    EVERY  SERVICE 


67 


L 

UN 

I  ON 

ST 

EAM 

P 

UM 

P 

C 

OM 

PANY 

4 

Loss  of  Work  Due  to  Heat   in   Compressing    Air 

From  Atmospheric   Pressure   to   Various 

Gauge  Pressures  by  Simple  and 

Compound   Compression 

Air  in  Each  Cylinder;  Initial  Temperature  60°  F. 


Gauge 
Pressure 

One  Stage 

Two  Stage 

Three  Stage 

Four  Stage 

Percentage  of  Work  Lost  in  Terms  of 

d 

£  a 

Adiabatic 
Compression 

Isothermal 
Compression 

1  Adiabatic 
Compression 

Isothermal 
Compression 

1  Adiabatic 
Compression 

Isothermal 
Compression 

|  Adiabatic 
Compression 

60 

29.9 

23.0 

13.4 

11.8 

8.6 

7.9 

4.7 

4.5 

70 

30.6 

23.4 

14.1 

12.4 

8.7 

8.0 

6.1 

5.7 

80 

32.7 

24.6 

14.7 

12.8 

9.7 

8.9 

6.4 

6.0 

90 

34.7 

25.8 

16.1 

13.8 

10.5 

9.5 

7.3 

6.8 

100 

36.7 

26.8 

16.9 

14.5 

10.9 

9.8 

7.8 

7.3 

125 

41.1 

29.2 

18.5 

15.6 

11.6 

10.4 

8.8 

8.1 

150 

44.8 

30.9 

20.1 

16.7 

12.3 

10.9 

9.1 

8.4 

200 

51.2 

33.9 

22.2 

18.1 

14.0 

12.3 

10.5 

9.5 

300 

61.2 

37.9 

25.7 

20.5 

16.6 

14.2 

12.0 

10.7 

400 

68.7 

40.7 

28.9 

22.4 

18.2 

15.4 

13.1 

11.5 

600 

70.6 

41.4 

31.2 

23.8 

19.3 

16.2 

14.1 

12.3 

600 

80.4 

44.5 

32.8 

24.7 

20.4 

16.9 

14.9 

13.0 

700 

85.0 

46.0 

34.6 

.25.7 

21.3 

17.6 

16.1 

13.8 

800 

89.5 

47.2 

35.7 

26.3 

22.0 

18.1 

16.2 

13.9 

900 

93.0 

48.2 

37.1 

27.0 

22.6 

18.5 

16.6 

14.4 

1000 

96.1 

49.0 

27.9 

27.5 

23.2 

18.8 

16.9 

14.5 

1200 

102.8 

50.7 

40.3 

28.8 

24.8 

19.9 

17.7 

15.0 

1400 

108.6 

52.0 

41.5 

29.3 

25.9 

20.5 

18.6 

15.7 

1600 

113.4 

53.1 

43.5 

30.3 

26.5 

20.9 

19.2 

16.1 

1800 

117.5 

54.0 

44.8 

31.0 

27.3 

21.2 

19.6 

16.4 

2000 

122.0 

55.0 

45.8 

31.4 

27.5 

21.5 

19.9 

16.5 

E.  F.    SCHAEFER. 


68 


BATTLE      CREEK.     MICHIGAN. U.  S.  A. 


Table  of  Volumes,  Mean  Pressures, 
Temperatures,  Etc. 

IN  THE  OPERATION  OF 

Air  Compression  from  One  Atmosphere 
and  60  Deg.  F. 


Gauge 
Pressure 

Absolute 
Pressure 

Pressuie 
in 
Atmos- 
pheres 

Volume  with 
Air  at 
Constant 
Temperature 

Volume 
with  Air 
not 
Cooled 

Mean  Pressure 
per  Stroke. 
Air  at 
Constant 
Temperature 

Mean  Pressure 
per  Stroke. 
Air  not  cooled 

Final  Temper-  II 
atures. 
Air  not  cooled  || 

11 

0 

14.7 

1. 

i. 

1. 

0. 

0. 

60 

0 

5 

19.7 

1.34 

.7462 

.81 

4.3 

4.5 

106 

5 

10 

24.7 

1.68 

.5952 

.69 

7.62 

8.27 

145 

10 

15 

29.7 

2.02 

.495 

.606 

10.33 

11.51 

178 

15 

20 

34.7 

2.36 

.4237 

.543 

12.62 

14.4 

207 

20 

25 

39.8 

2.7 

.3703 

.494 

14.59 

17.01 

234 

25 

30 

44.7 

3.04 

.3289 

.4638 

16.34 

19.4 

255 

30 

35 

49.7 

3.381 

.2957 

.42 

16.92 

21.6 

281 

35 

40 

54.7 

3.721 

.2687 

.393 

19.32 

23.66 

302 

40 

45 

59.7 

4.061 

.2462 

.37 

20.52 

25.59 

321 

45 

50 

64.7 

4.401 

.2272 

.35 

21.79 

27.39 

339 

50 

55 

69.7 

4.741 

.2109 

.331 

22.77 

29.11 

357 

55 

60 

74.7 

5.081 

.1968 

.3144 

23.84 

30.75 

375 

60 

65 

79.7 

5.423 

.1844 

.301 

24.77 

31.69 

389 

65 

70 

84.7 

5.762 

.1735 

.288 

26. 

33.73 

405 

70 

75 

89.7 

6.102 

.1639 

.276 

26.65 

35.23 

420 

75 

80 

94.7 

6.442 

.1552 

.267 

27.33 

36.6 

432 

80 

85 

99.7 

6.782 

.1474 

.2566 

28.05 

37.94 

447 

85 

90 

104.7 

7.122 

.1404 

.248 

28.78 

39.18 

459 

90 

95 

109.7 

7.462 

.134 

.24 

29.53 

40.4 

472 

95 

100 

114.7 

7.802 

.1281 

.232 

30.07 

41.6 

485 

100 

105 

119.7 

8.142 

.1228 

.2254 

30.81 

42.78 

496 

105 

110 

124.7 

8.483 

.1178 

.2189 

31.39 

43.91 

507 

110 

115 

129.7 

8.823 

.1133 

.2129 

31.98 

44.98 

508 

115 

120 

134.7 

9.163 

.1091 

.2073 

32.54 

46.04 

529 

120 

125 

139.7 

9.503 

.1052 

.202 

33.07 

47.06 

540 

125 

130 

144.7 

9.843 

.1015 

.1969 

33.57 

48.1 

550 

130 

135 

149.7 

10.183 

.0981 

.1922 

34.05 

49.1 

560 

135 

140 

154.7 

10.523 

.098 

.1878 

34.57 

50.02 

570 

140 

145 

159.7 

10.846 

.0921 

.1837 

35.09 

51. 

580 

145 

150 

164.7 

11.204 

.0892 

.1796 

35.48 

51.89 

589 

150 

AND   CONDENSERS    FOR   EVERT  SERVICE 


UNION       STEAM      PUMP       CO 

M 

PANY    _Jj 

Efficiencies  of  Air  Compression  at  Different 
Altitudes 


Barometric  Pressure 

Volumetric 

Loss  of 

Decreased 

Altitude 

Efficiency 

Capacity 

Power 

Inches 

Pounds  per 

Compressor 
Per  Cent 

Per  Cent 

Required 
Per  Cent 

Mercury 

Sq.  Inch 

0 

30.00 

14.75 

100 

0 

0. 

1000 

28.88 

14.20 

97 

3 

1.8 

2000 

27.80 

13.67 

93 

7 

3.5 

3000 

26.76 

13.16 

90 

10 

5.2 

4000 

25.76 

12.67 

87 

13 

6.9 

6000 

24.79 

12.20 

84 

16 

8.5 

6000 

23.86 

11.73 

81 

19 

10.1 

7000 

22.97 

11.30 

78 

22 

11.6 

8000 

22.11 

10.87 

76 

24 

13.1 

9000 

21.29 

10.45 

73 

27 

14.6 

ieooo 

20.49 

10.07 

70 

30 

16.1 

11000 

19.72 

9.70 

68 

32 

17.6 

12000 

18.98 

9.34 

65 

35 

19.1 

13000 

18.27 

8.98 

63 

37 

20.6 

14000 

17.59 

8.65 

60 

40 

22.1 

15000 

16.93 

8.32 

•58 

42 

23.5 

Density  of  Gases  and  Vapors 

Compared  with  air  at  same  temperature  and  pressure;  also  weight  of  a 
cubic  foot  at  62°  F.  under  atmospheric  pressure  of  14.7  Ibs.  abs.  or  29.92 
inches  mercury. 


Density,  Air 
at  same  temp, 
and  pres.  be- 
ing 1.0  (Reg- 
nault) 

Specific  Gravity 
or  Density,  Water 
at  62°  being  1.0 

Wt.  of  a 
Cu.  Foot 
in  Pounds 

Cubic  Feet 
at  62°  in 
One  Pound 

Air  (atmospheric)  
Hydrogen  gas  

1.00000 
.06926 

.001221     or     *h 
.0000846  or  Tjl25 

.07610 
.00527 

13.14 
189.70 

Oxygen  gas  
Nytrogen  gas 

1.10563 
97137 

.001350     or     TJT 
001185     or     -ski 

.08414 
07383 

11.88 
13  54 

Carbonic  acid  gas  
Carbonic  oxide  gas  
Vapor  of  water  

1.52901 
.9674 
.6235. 

.001870     or     sJ5 
.00118       or     *27 
.0007613  or  T3}3 

.11636 
.07364 
.04745 

8.59 
13.60 
21.07 

Vapor  of  alcohol  
Vapor  of  sulphuric  ether  
Vapor  of  oil  of  turpentine.  .  .  . 
Vapor  of  mercury  

1.589 
2.586 
4.760 
6.976 

.00194       or     sJs 
.00316       or     . 
.00581       or     T$g 
.00850       or     T}s 

.12092 
.  19680 
.36224 
.52987 

8.27 
5.08 
2.76 

1.88 

Effect   of   Initial   or  Intake  Temperature  on  Effi- 
ciency and  Capacity  of  Air  Compressors 

Unit  Capacity  and  Efficiency  Assumed  at  60°  F. 


Initial  Temperature 

Initial  Temperature 

Relative 

Relative 

Degrees 
Fahr. 

Degrees 

Abs. 

Capacities  and 
Efficiencies 

Degrees 
Fahr. 

Degrees 

Abs. 

Capacities 
and 
Efficiencies 

20 

441 

1.18 

70 

583 

.980 

10 

451 

1.155 

80 

541 

.961 

0 

461 

1.13 

90 

551 

.914 

10 

471 

1.104 

100 

561 

.928 

20 

481 

1.083 

110 

571 

.912 

30 

491 

1.061 

120 

581 

.896 

32 

493 

1.058 

130 

591 

.880 

40 

501 

1.040 

140 

601 

.866 

50 

511 

1.020 

150 

611 

.852 

60 

521 

1.000 

160 

621 

.838 

PUMPING    MACHINERY,    AIRCOMPRESS  ORS. 


70 


B  ATTLE      C  REBK.     MICHIGAN,      U.S.A. 

Bri....idlj..*.».».**mBBnre^^V»»i*f"™ti»y«tfaEirinfr^ 


Multipliers  to   be  Used   for  Transforming  Vol- 
umes  of   Compressed   Air  at  Various  Pres- 
sures Into  Corresponding  Volumes  of 
Free  Air   at  Atmospheric  Pres- 
sure  of    14.7    Pounds 


s 

iS 

i 

ji 

Jj 

<u 

JH 

.53 

i 

CL> 

K 

|H 

V 

0? 

IH 

i| 

B 

IH 
B 

3 

£ 

w 

.9* 

Cft 

o. 

w 

.2* 

3 

.8* 

1 

3 

1 

3 

w 

(£ 

3 

1 

3 

1 

.   "§ 

1 

1.068027 

26 

2  .  768602 

51 

4.469377 

76 

6.170052 

101 

7.870727 

2 

1  .  136054 

27 

2.836729 

52 

4  .  537404 

77 

6.238079 

102 

7.938754 

3 

1  .  204081 

28 

2.904756 

53 

4.60543.1 

78 

6.306106 

103 

8.006781 

4 

1.272108 

29 

2.927783 

54 

4.673458 

79 

6.374133 

104 

8.074808 

5 

1.340135 

30 

3.040810 

55 

4.741485 

80 

6.442160 

105 

8.142835 

6 

1.408162 

31 

3.108837 

56 

4.809512 

81 

6.510187 

106 

8.210862 

7 

1.476189 

32 

3.176864 

57 

4.877539 

82 

6.578214 

107 

8  .  278889 

8 

1.544216 

33 

3.244891 

58 

4.945566 

83 

6.646241 

108 

8.346916 

9 

1.612243 

34 

3.312918 

59 

5.013593 

84 

6.714268 

109 

8.414943 

10 

1  .  680270 

35 

3.380945 

60 

5.081620 

85 

6.782295 

110 

8  .  482970 

11 

1  .  748297 

36 

3.448972 

61 

5.149647 

86 

6.850322 

12 

1.816324 

37 

3.516999 

62 

5.217674 

87 

6.918349 

13 

1.884351 

38 

3.585026 

63 

5.285701 

88 

6.986376 

*t 

14 

1.952378 

39 

3  .  653053 

64 

5.353728 

89 

7  .  054403 

3 

15 

2.020405 

40 

3.721080 

65 

5.421755 

90 

7.122430 

+   cu 

16 

2  .  088432 

41 

3.789107 

66 

5.489782 

91 

7.190457 

«u-  ^ 

17 

2.156459 

42 

3.857134 

67 

5.557809 

92 

7.258484 

£   3  '-£ 

18 

2.224486 

43 

3.925161 

68 

5.625836 

93 

7.326^11 

19 

2.292513 

44 

3.993188 

69 

5.693863 

94 

7.394538 

•g  i  1 

20 

2.360540 

45 

4.061215 

70 

5.761890 

95 

7.462565 

I  *  ii 

21 

2.428567 

46 

4.129242 

71 

5.829917 

96 

7.530592 

fe  X 

22 

2.496594 

47 

4.197269 

72 

5.897944 

97 

7.598619 

23 

2.564621 

48 

4.265296 

73 

5.965971 

98 

7.666646 

•H  ^ 

24 

2.632648 

49 

4.333323 

74 

6.033998 

99 

7.734673 

i-H 

25 

2.700675 

50 

4.401350 

75 

6.102025 

100 

7.802700 

Atm.  Press.  14.7  pounds  =  30  "  Barom.  Press.     Temp.  60°  P. 


71 


a 

g 

o 
U 


c/3 

o 


H 


. 
»3*2 


ft         o 


DIM 

o  c  0+3 

**O 


l     l 


lii'fi* 

aw 


Per  Cent  of 
Efficiency  of 
Air  Considering 
its  Volume  100 
Per  Cent  at 
Sea  Level 


etric 
ure 


Ba 
P 


O 


§ 


m 

OH      ^ 


I 


jj 


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72 


ATTLE      CREEK.     MICHIGAN 


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Compressed  Air  Table  for  Hoisting  Engines 

The  following  table  is  intended  to  give  an  approximate 
idea  of  the  volume  of  free  air  required  for  operating  hoisting 
engines,  the  air  being  delivered  to  the  engines  at  60  pounds 
gauge  pressure.  There  are  so  many  variable  conditions  in  the 
operation  of  hoisting  by  the  hoisting  engines  in  common  use, 
that  accurate  computations  can  only  be  offered  when  fixed 
data  are  given.  In  the  table,  the  hoisting  engine  is  assumed 
to  actually  run  but  one-half  of  the  time  for  hoisting,  while  the 
compressor,  of  course,  runs  continuously.  If  the  engine  runs 
less  than  one-half  the  time,  as  it  usually  does,  the  volume  of 
air  required  will  be  proportionately  less,  and  vice  versa.  The 
table  is  computed  for  maximum  loads,  which  also  in  practice 
may  vary  widely.  From  the  intermittent  character  of  the 
work  of  a  hoisting  engine,  the  parts  are  able  to  resume  their 
normal  temperature  between  the  hoists,  and  there  is  little 
probability  of  the  annoyance  of  freezing  up  the  exhaust  passages. 

Table  of   the  Volume  of   Free  Air   Required   for 
Operating  Hoisting  Engines 

The  Air  Compressed  to  60  Pounds  Gauge  Pressure. 


SINGLE  CYLINDER  HOISTING  ENGINE 


Diameter 
of 
Cylinder, 
Inches 

Stroke, 
Inches 

Revolutions 
per 
Minute 

Normal 
Horse- 
Power 

Actual 
Horse- 
Power 

Weight 
Lifted 
Single  Rope 

Cubic  Feet 
of  Free  Air 
Required 

5 

6 

200 

3 

5.9 

600 

75 

5 

8 

160 

4 

6.3 

1000 

80 

6/4 

8 

160 

6 

9.9 

1500 

125 

7 

10 

125 

10 

12.1 

2000 

151 

8/4 

10 

125 

15 

16.8 

3000 

170 

8/^ 

12 

110 

20 

18.9 

5000 

238 

10 

12 

110 

25 

26.2 

6000 

330 

DOUBLE  CYLINDER  HOISTING  ENGINE 


5 

6 

200 

6 

11.8 

1000 

150 

5 

8 

160 

8 

12.6 

1650 

160 

6M 

8 

160 

12 

19.8 

2500 

250 

10 

125 

20 

24.2 

3500 

302 

8M 

10 

125 

30 

33.6 

6000 

340 

8K 

12 

110 

40 

37.8 

8000 

476 

10 

12 

110 

50 

52.4 

10000 

660 

121^ 

15 

100 

75 

89.2 

1125 

i&  y^ 

14 

18 

90 

100 

125 



1587 

•ING    MACHINERY,    AIR   COMPRESSORS 

»*»•» •»»•««»  iv  a  ugttguutilrrrgg^g^^aTy-irTnfTreTgff^^^ 


74 


BATTLE      CREEK,     MICHIGAN.      U.S.A. 


Air  Used  in  Cubic  Feet  Free  Air  Per  Minute 

Per  Indicated  Horse-power  in  Motors 

(Without  Reheating) 


Point 


Gauge  Pressure  *in  Pounds 


of 

Cut- 

30 

40 

50 

60 

70 

80 

90 

100 

no 

125 

150 

off 

1 

23.3 

21.3 

20.2 

19.4 

18.8 

18.42 

18.10 

17.8 

17.62 

17.40 

17.05 

34 

18.7 

17.1 

16.1 

15.47 

15.0 

14.6 

14.35 

14.15 

13.98 

13.78 

13.50 

2A 

17.85 

16.2 

15.2 

14.50 

14.2 

13.75 

13.47 

13.28 

13.08 

12.90 

12.60 

16.4 

14.5 

13.5 

12.8 

12.3 

11.93 

11.7 

11.48 

11.30 

11.10 

10.85 

% 

17.5 

15.2 

12.9 

11.85 

11.26 

10.8 

10.5 

10.21 

10.02 

9.78 

9.50 

1A 

20.6 

15.6 

13.4 

13.3 

11.40 

10.72 

10.31 

10.0 

9.75 

9.42 

9.10 

As  will  be  seen  from  the  table,  the  only  data  required  are  the  gauge 
pressure  and  point  of  cut-off;  given  those  two  items,  we  find  from  the  table 
the  free  air  required  per  indicated  horsepower,  and  it  will  only  be  neces- 
sary to  multiply  this  amount  by  the  total  indicated  horse  power  of  the 
motor,  to  determine  the  total  quantity  of  free  air  required,  and  conse- 
quently the  necessary  size  of  an  air  compressor  to  furnish  the  required 
amount  of  air. 

These  figures  do  not  take  account  of  clearance,  but  it  will  be  an  easy 
matter  to  add  the  per  cent  of  clearance  after  having  determined  the  total 
amount  of  free  air  required. 

It  will  also  be  noticed  that  the  free  air  consumption  is  based  upon 
the  use  of  cold  air,  i.  e.,  initial  temperature  of  air  at  60  degrees  Fahr. 
In  case  reheating  is  resorted  to,  there  will  be  a  corresponding  decrease  in 
the  amount  used,  dependent  upon  the  temperature  of  air  on  admission  to 
motor,  and  will  be  proportional  to  the  ratio  of  ^  where  T2  =  460  plus 
60=520  degrees  Fahr.  absolute  temperature  and  T3  =460  plus  tempera- 
ture of  air  at  admission  to  motor. 

Thus,  if  the  air  is  reheated  to  300  degrees  Fahr.,  the  quantity  in  the 
table  will  have  to  be  multiplied  by 


460+60 


460+300 


520 


760 


=   .684 


A  further  use  of  this  table  is  to  find  the  most  economical  point  of 
cut-off  for  gauge  pressures  from  30  pounds  to  150  pounds  per  square  inch. 
This  fact  is  apparent  from  a  study  of  each  vertical  column:  thus,  at  60 
pounds  pressure,  the  lowest  consumption  of  free  air  per  indicated  horse 
power  is  at  1-3  cut-off,  while  at  40  pounds  pressure  the  most  economical 
cut-off  will  be  /. 


AND    CONDENSERS    FOR   EVERT  SERVICE 


Volume  of  Air  and    Pressure  Required   to   Drive 
Direct  Acting  Steam  Pumps 

From  Hiscox's  "Compressed  Air" 


Gauge  Pressure  in  Pounds 

Cubic  Feet  of  Free  Air  per  Minute 

lH 
$ 

per  Square  Inch 

to  Lift  One  Gallon  of  Water 

£ 

Ratio  of  Cylinder  Diameters 

Ratio  of  Cylinder  Diameters 

;i 

1 

1M 

IK 

1M 

2 

2H|    3 

1 

IK 

1H 

I& 

2 

2K 

3 

s* 

to 

to 

to 

to 

to 

to      to 

to 

to 

to 

to 

to 

to 

to 

w.s 

1 

1 

1 

1 

1 

1    j    1 

1 

1 

1 

1 

1 

1 

1 

10 

6 

22 

20 

11 

7 

.28 

.37 

30 

16 

10 

7 

.33 

.42 

.53 

40 

21 

13 

9 

7 

.38 

.47 

.58 

.72 

50 

26 

17 

12 

9 

7 

.44 

.53 

.65 

.79 

.94 

60 

31 

20 

14 

10 

8 

.49 

.58 

70 

.82 

.99 

70 

36 

23 

16 

12 

9 

.54 

.63 

.75 

.88 

1.03 

80 

42 

26 

18 

14 

11 

.61 

.68 

.79 

.95 

1.11 

90 

47 

30 

21 

15 

12 

.66 

.75 

.87 

.98 

1.15 

100 

52 

34 

23 

17 

13 

.72 

.82 

.91 

1.05 

1.20 

125 

65 

42 

29 

21 

16 

10 

.86 

.95 

1.06 

.18 

1.33 

1.67 

150 

78 

50 

35 

25 

20 

13 

9 

1.00 

1.08 

1.20 

.31 

1.50 

1.88 

2.31 

175 

90 

58 

40 

30 

23 

15 

10 

1.12 

1.22 

1.32 

.47 

1.63 

2.00 

2.40 

200 

105 

67 

46 

34 

26 

17 

12 

1.28 

1.37 

1.47 

.60 

1.75 

2.14 

2.60 

250 

83 

58 

42 

33 

21 

15 

1.64 

1.75 

.86 

2.06 

2.41 

2.89 

300 

100 

68 

50 

39 

25 

17 

1.92 

2.00 

2.12 

2.31 

2.68 

3.08 

350 

.  .  .  . 

80 

58 

45 

29 

20 

2.28 

2.39 

2.57 

2.95 

3.37 

400 

99 

67 

59 

33 

23 

9  57 

9  68 

9  87 

}   99 

3  66 

450 

105 

75 

58 

37 

26 

9  88 

9  94 

3   13 

3  48 

3  95 

500 

85 

65 

49 

29 

3  97 

3  49 

3  89 

4  24 

600 

100 

78 

50 

35 

3  76 

4  00 

4  35 

4.80 

700 

92 

60 

42 

4   58 

5  00 

5  50 

800 

105 

67 

47 

5   15 

5  50 

5  96 

900 

75 

52 

6  00 

6  45 

1000 

85 

58 

6.70 

7.00 

To  find  the  quantity  of  free  air  required  per  minute,  in  a  direct  acting 
steam  pump,  to  raise  a  given  number  of  gallons  of  water  through  a  given 
head,  divide  the  diameter  of  the  air  cylinder  by  the  diameter  of  the  water 
cylinder,  and  under  the  heading  of  this  ratio  in  above  table,  and  to  the 
right  of  the  given  head  or  lift,  find  the  cubic  feet  of  free  air  per  gallon 
required  per  minute;  this  constant,  multiplied  by  the  total  number  of 
gallons  to  be  lifted,  will  give  the  quantity  of  free  air  required.  The  gauge 
pressure  for  the  corresponding  conditions  may  be  found  in  a  similar  man- 
ner under  the  heading  of  gauge  pressures. 

In  the  foregoing  table  of  pressures  an  allowance  of  15  per  cent  has 
been  made  for  pump  friction,  and  in  the  table  of  volumes  15  per  cent  has 
also  been  allowed  for  clearance  losses  and  leakage  .  If  the  air  is  reheated 
before  admission  to  air  cylinder,  the  quantity  may  be  reduced  in  propor- 
tion to  the  ratio  of  absolute  temperatures.  For  compound  pumps  the 
consumption  may  be  assumed  at  75  per  cent  of  the  best  results  of  the  above 
table. 


B  A  T  T  L  E      CREEK.     MICHIGAN.     U.S.  A. 


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PUMPING   MACHINER.T,    AIR   COMPRESSORS 


78 


c 

B 

ATTLE 

C 

RE 

EK. 

M 

ICH 

IGAN, 

U. 

S.  A. 

3 

Contents  of  Cylinder  in  Cubic  Feet  for 
Each  Foot  in  Length 


Diameter 
in  Inches 

Cubic 
Contents 

Diameter 
in  Inches 

Cubic 
Contents 

Diameter 
in  Inches 

Cubic 
Contents 

i  Diameter 
in  Inches 

Cubic 
Contents 

Diameter 
in  Inches 

Cubic 
Contents 

1 

.0055 

6 

.1963 

11 

.6600 

20 

2.182 

36 

7.069 

1M 

.0085 

6K 

.2130 

11M 

.6903 

20  % 

2.292 

37 

7.468 

ilA 

.0123 

61A 

.  2305 

ny2 

.7213 

21 

2.405 

38 

7.88^ 

1% 

.0168 

6% 

.2485 

n% 

.7530 

21^ 

2.521 

39 

8.296 

2 

.0218 

7 

.2673 

12 

.7854 

22 

2.640 

40 

8.728 

2M 

.0276 

7^ 

.2868 

12^ 

.8523 

22^ 

2.761 

41 

9.168 

2^ 

.0341 

7y2 

.3068 

13 

.9218 

23 

2.885 

42 

9.620 

2M 

.0413 

7% 

.3275 

13^ 

.9940 

23^ 

3.012 

43 

10.084 

3 

.0491 

8 

.3490 

14 

1.069 

24 

3.142 

44 

10.560 

3M 

.0576 

8M 

.3713 

14^ 

1.147 

25 

3.409 

45 

11.044 

3^ 

.0668 

8^ 

.3940 

15 

1.227 

26 

3.687 

•46 

11.540 

3M 

.0767 

8^i 

.4175 

15^ 

.310 

27 

3.976 

47 

12.048 

4 

.0873 

9 

.4418 

16 

.396 

28 

4.276 

48 

12.566 

4^ 

.0985 

9M 

.4668 

16^ 

.485 

29 

4.587 

4^ 

.1105 

9^ 

.4923 

17 

.576 

30 

4.909 

4M 

.1231 

9M 

.5185 

17^ 

.670 

31 

5.241 

5 

.1364 

10 

.5455 

18 

.767 

32 

5.585 

5M 

.1503 

10M 

.5730 

18^ 

1.867 

33 

5.940 

5H 

.1650 

10H 

.6013 

19 

1.969 

34 

6.305 

5% 

.1803 

10% 

•  .6303 

19^ 

2.074 

35 

6.681 

To  ascertain  the  piston  displacement  of  an  air  compressor,  multiply 
the  cubic  contents  stated  opposite  its  diameter  (second  column)  by  the 
piston  travel  in  feet  per  minute.  The  result  will  be  the  theoretical  ca- 
pacity of  each  double-acting  cylinder,  or  one-half  of  the  result  will  be  the 
theoretical  capacity  of  a  single-acting  cylinder. 


Table  of  Branch  Pipes 

Relative  Carrying  Capacity  of  Pipes  for  Air. 


B* 

1S 

1 

1W 

1H 

2 

2H 

3 

3K2 

4 

*y* 

5 

6 

7 

8 

10 

12 

1 

1.00 
1  90 

.52 

1.00 

.327 
.614 

.15 

.28 

.084 
.16 

.05 
.10. 

.066 

1  i4 

3.05 

1.60 

1.00 

.46 

.256 

.16 

.106 

.075 

2 

6.55 

3.45 

2.14 

1.00 

.56 

.34 

.23 

.160 

.12 

2  3^ 

11.8 

6.25 

3.88 

1.81 

1.00 

.614 

.41 

.29 

.216 

.163 

3 

19.0 

12.0 

6  32 

2  95 

1.63 

1.00 

.67 

.47 

.35 

.268 

.165 

3H 



15.2 

9.45 

4.3 

2.43 

1.50 

1.00 

.71 

.52 

.400 

.246 

.166 

4: 



21.6 

13.4 

6.25 

3.46 

2.10 

1.42 

1.00 

.75 

.56 

.352 

.237 

169 

4  J^ 



18.0 

8.30 

4.65 

2.85 

1.90 

1.35 

1.00 

.76 

.475 

.32 

227 

,128 

5 

6  14 

3  77 

2  60 

1  78 

1  32 

1  00 

625 

42 

30 

169 

10 

6 

6  05 

4  00 

2  85 

2  15 

1  60 

I  00 

675 

48 

27 

17 

7 

6  00 

4  20 

3  16 

2  37 

1  48 

1  00 

71 

40 

25 

8 

6  00 

4  40 

3  25 

2  10 

1  40 

1.00 

56 

.35 

10 

7  85 

5  90 

3  70 

2  50 

1  77 

1  00 

63 

12 

9  40 

5.90 

3.95 

2.80 

1  60 

1.00 

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Globe  Valves,  Tees  and  Elbows 

The  reduction  of  pressure  produced  by  globe  valves  is  the 
same  as  that  caused  by  the  following  additional  lengths  of 
straight  pipe,  as  calculated  by  the  formula: 

1 14  X  diameter  of  pipe 
Additional  length  of  pipe  =  — 

1  +  (3.6  =  diameter) 

Diameter  of  pipe  }  1        ll/2   2       2^    3       3X    4       5        6  ins. 
Additional  length  j  2       4       7       10      13     16      20     28      36ft. 

7       8  .    10     12     15     18     20     22     24  ins. 
44     53     70     88     115  143  162  181  200  ft. 

The  reduction  of  pressure  produced  by  elbows  and  tees  is 
equal  to  two-thirds  of  that  caused  by  globe  valves.  The  follow- 
ing are  the  additional  lengths  of  straight  pipe  to  be  taken  into 
account  for  elbows  and  tees.  For  globe  valves,  multiply  by  -f : 

Diameter  of  pipe  )   1        I1/*   2       2%  3       3K  4    .    5       6     ins. 
Additional  length  [  2       3       5       7       9      11     13     19     24  ft. 

7       8       10     12     15     18     20     22     24  ins. 
30     35     47     59     77     96     108  120  134  ft. 

These  additional  lengths  of  pipe  for  globe  valves,  elbows 
and  tees  must  be  added  in  each  case  to  the  actual  length  of 
straight  pipe.  Thus  a  6-inch  pipe,  500  feet  long,  with  1  globe 
valve,  2  elbows  and  3  tees,  would  be  equivalent  to  a  straight 
pipe  500  +  36  +  (2  X  24)  +  (3  X  24)  =  656  feet  long. 


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PUMPING    MACHINERY,    AIR    COMPRESSjORS 


86 


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Air     Consumption    of    Various    Types   of    Tools 
and    Machines 


Tools 

Size 

Air   Pressure  in 
in  Pounds 
per  Square  Inch 

Air  Consumed, 
Free  Air  per  Min. 
(Cubic  Feet) 

Aerons 
(Paint  Sprays) 

Small  Hand 

90 

2-7 

Chipping 
Hammers 

Weight  Pounds 
5 
7 
8 
9 
10 
11 
12 
13 
14 
18 

90 
90 
90 
90 
90 
90 
90 
90 
90 
90 

9 
12 
15 

15K 
16 
17 
18 
20 
20 
22 

Foundry 
Jolting 
Machines 

Platform 

type 

80 

Air  per  ton 
lifting  capacity 
30-40 

Grinders 
(Hand) 

Weight  Pounds 
17 
24 

80 
80 

20 
30 

Cylinder 
Air  Hoists 
Direct  Lift 

(Cylinder) 
Diam.  inches 
6 
8 
10 
12 
14 
17 
19 

80 
80 
80 
80 
80 
80 
80 

Free  air  in  cu.  ft. 
per  min.  per  ft.  lift 
1.22 
2.24 
3.29 
5.06 
7.13 
10.10 
12.50 

Cylinder 
Air  Hoists 
Rope-Geared 
2-1 

6 
8 
10 
12 
14 
17 
19 

80 
80 
80 
80     • 
80 
80 
80 

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1.12 
1.65 
2.53 
3.57 
5.05 
6.25 

Air  Motor 
Hoists 

Tons  Capacity 

IK 
2 
3 
4 
5 
6 
8 
10 

80 
80    , 
80 
80 
80 
80 
80 
80 
80 

4 
6 
8 
9 
12 
15 
19 
25 
30 

Air  Consumption  is  shown  in  terms  of  "Free  Air." 


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Centrifugal 
Pumps 


fz. 


SECTION  TWO 


Centrifugal    Pumps 

For  many  years  the  centrifugal  pump,  which  is  the  simplest 
type  of  pumping  machine,  undeveloped  and  crude  in  design  and 
construction,  was  used  only  for  pumping  against  comparatively 
low  heads,  and  where  economy  was  of  secondary  importance. 
In  recent  years,  however,  a  great  advance  has  been  made  in  the 
design  and  construction  of  centrifugal  pumps;  and  the  higher 
degree  of  economy  now  secured,  both  at  high  and  low  heads, 
also  the  vise  of  the  turbine  pump  constructed  in  multiple  stages, 
have  brought  the  centrifugal  pump  into  general  use  for  a  vast 
variety  of  purposes.  Formerly  it  was  not  thought  possible  to 
operate  centrifugal  pumps  at  heads  greater  than  20  or  30  feet 
with  any  degree  of  economy,  but  with  the  remarkable  progress 
that  has  been  made  in  both  the  theory  and  design,  it  is  now 
possible  to  build  economical  pumps  for  heads  up  to  300  feet 
per  stage. 

In  a  centrifugal  pump,  the  mechanical  power  delivered  to 
the  shaft  by  the  prime-  mover  is  transmitted  to  the  water  by 
means  of  a  series  of  radial  vanes  cast  together  to  form  a  single 
element  called  an  impeller,  and  revolved  by  the  shaft.  The 
water  is  led  to  the  inner  ends  of  the  impeller  vanes  which  pick 
it  up  with  a  rapidly  accelerating  motion  causing  it  to  flow  radially 
between  them  so  that  when  reaching  the  outer  circumference 
of  the  impeller,  the  water,  owing  to  the  velocity  and  pressure 
acquired,  has  absorbed  all  of  the  power  transmitted  to  the  pump 
shaft;  thus  the  problem  to  be  solved  in  impeller  design  is  to 
obtain  the  acquired  velocity  and  pressure  with  a  minimum  loss 
in  shock  and  friction.  Since  the  energy  of  the  water  on  leaving 
the  pump  is  required  to  be  mostly  in  the  form  of  a  pressure, 
the  next  problem  is  to  transform  into  pressure  the  kinetic  energy 
of  the  water  due  to  its  velocity  on  leaving  the  impeller,  and  to 
accomplish  it  with  the  least  possible  loss. 

The  accomplishment  of  this  is  the  function  of  the  casing 
which  may  be  of  the  volute  type,  or  the  circular  type  with 
diffusion  vanes.  The  change  from  velocity  to  pressure  is  ac- 
complished by  slowing  down  the  speed  of  the  water,  and  it  is 
necessary  that  this  change  take  place  gradually  and  uniformly, 
with  the  least  loss  from  eddies  and  shock.  With  a  proper  design 
of  volute  or  diffusor,  it  is  possible  to  transform  practically  the 
whole  of  the  velocity  into  pressure  so  that  the  loss  from  this 
source  is  very  small. 


90 


Impellers 


Enclosed  Impeller  Fig.  39  Open  Impeller 

There  are  two  general  forms  of  impellers  which  are  known  as 
the  open  and  enclosed  type. 

The  former  consists  of  a  set  of  radial  vanes  attached  to  the 
central  hub  and  disk,  and  open  at  the  sides,  the  whole  revolving 
between  the  two  fixed  side  plates  of  the  pump,  while  in  the  latter 
the  vanes  are  formed  between  two  circular  disks  which  form 
closed  passages  between  the  vanes  and  extend  from  the  inlet 
opening  to  the  outer  periphery  of  the  impeller.  Since  the  open 
impeller  revolves  between  the  two  stationary  disks,  it  is  necessary 
to  allow  some  clearance  on  each  side  to  prevent  contact,  with  the 
result  that  there  is  considerable  leakage  at  these  extended  points 
and  a  consequent  loss  of  efficiency.  The  water  passing  through 
the  impeller  is  revolved  against  these  stationary  side  plates  with 
a  velocity  approximately  the  same  as  that  of  the  vanes,  and  there- 
fore offers  a  frictional  resistance  proportional  to  the  square  of 
this  velocity.  In  the  enclosed  impeller  there  can  be  no  leakage 
by  the  sides  of  the  vanes.  The  only  possible  leakage  being 
around  the  outside  of  the  impeller  into  the  suction,  and  this  is 
practically  prevented  from  occuring  by  means  of  a  running  fit 
around  the  inlet  opening.  The  frictional  loss  of  an  enclosed 
impeller  is  caused  only  by  the  outer  surface  revolving  in  the  sur- 
rounding water.  Since  the  frictional  loss  of  the  impeller  is  the 
principal  loss  in  the  centrifugal  pump/  it  is  evident  that  any 
saving  at  this  point  will  greatly  improve  the  efficiency  of  the 
pump.  For  these  reasons  the  enclosed  impeller  is  used  more 
extensively  than  the  open  impeller  and  particularly  in  efficient 
pumps.  The  open  impeller  is  particularly  adapted  to  handling 
liquids  which  contain  sand,  grit,  or  other  foreign  matter. 


91 


J        UNION       S 

TE 

AM 

P 

UM 

P       COMPANY         | 

Turbine  and  Volute  Pumps 

Centrifugal  pumps  are  divided  inco  two  general  classes: 
Turbine  and  Volute  Pumps. 

The  Turbine  Pump 

The  turbine  pump  is  the  type  used  for  heads  higher  than 
250  feet.  With  this  type  of  pump,  100  feet  per  stage  usually 
gives  satisfactory  results,  but  it  is  possible  to  operate  on  heads 
up  to  300  feet  per  stage  without  difficulty,  depending  upon  the 
speed  available. 


Fig.  40.     Multistage  Turbine  Pump. 

The  turbine  pump  has  a  circular  casing,  and  has  diffusion 
vanes  which  surround  the  impeller.  These  diffusion  vanes  pro- 
vide gradually  enlarging  passages,  whose  function  it  is  to  reduce 
the  velocity  of  the  water  leaving  the  impeller,  and  efficiently 
transform  the  velocity  head  into  pressure  head. 


Fig.  42.     Diffusion  Vanes  of  Turbine  Pump. 


Fig.  189.      Multistage  Volute  Pump. 


Fig.  43.      Shaft  and  Rotating  Parts  of  Multistage  Pump. 

With  the  multistage  type  of   pump,  it  is  necessary  to  pro- 
vide a  balancing  device  to  take  up  the  end  thrust  of  the  impeller. 

Referring  to  the  accompanying  Fig.   44,   we  see  that  in 
space  A  and  B,  the  pressure  created  by  the  impeller  is  the  same. 


Fig.  44.      Hydraulic  Balancing  Device  for  Multistage  Volute  Pump. 


|         UNION 

S  TEAM 

PUMP 

COMPANY 

J| 

In  space  A,  the  surface  of  the  impeller  exposed  to  this 
pressure  is  shown  by  diameters  D  and  Dx.  In  space  B,  by  D  and 
D2.  But  as  diameter  D2  is  smaller  than  Dl  the  thrust  on  oppo- 
site sides  will  be  unequal  and  the  impeller  will  be  pushed  towards 
the  suction  side  of  the  pump. 

In  order  to  counterbalance  this  effect,  there  is  provided 
a  piston  C  which  receives  the  pressure  along  the  sleeve  E,  and  is 
of  such  diameter  as  to  produce  the  same  thrust  in  the  other 
direction  on  the  shaft  as  the  unbalanced  impellers. 

This  device  works  automatically,  for  should  the  thrust  of 
the  impellers  exceed  the  effect  of  the  piston,  the  space  F  will  be 
closed,  and  the  pressure,  therefore,  will  be  built  up.  This  pushes 
the  piston  away,  and  produces  a  leak,  whereupon  the  pressure 
drops,  and  the  shaft  moves  back  towards  the  suction  side.  By 
this  counteracting  of  pressure,  the  shaft  and  impeller  are  kept  in 
hydraulic  balance,  avoiding  end  thrust  on  the  shaft  bearings. 
As  there  is  a  continuous  leak  from  the  balancing  chambers,  the 
piston  does  not  run  directly  on  the  metallic  surfaces  of  the  casing, 
but  is  separated  from  the  latter  by  a  thin  film  of  water. 

The  amount  of  water  required  by  this  hydraulic  balancing 
device  ranges  from  %%  to  3%  of  the  capacity  of  the  pump; 
however,  the  water  used  is  not  included  in  the  rating  of  the 
pump,  as  the  capacity  of  the  pump  is  measured  by  the  quantity 
of  water  delivered  from  the  discharge  nozzle. 


The  Volute  Pump 

The  volute  pump  is  one  which  has  no  diffusion  vanes,  but 
instead  the  casing  is  of  the  spiral  type,  so  as  to  gradually  reduce 
the  velocity  of  the  water  as  it  flows  from  the  impeller  to  the  dis- 
charge pipe. 

The  volute  pump  is  made  in  both  the  single-stage  and 
multistage  types.  These  pumps  are  used  for  all  services  for 
which  centrifugal  pumps  are  suitable  and  the  operating  head 
varies  with  single  stage  pumps  up  to  250  feet,  and  in  the  multi- 
stage types  up  to  1,000  feet. 


||        BATTLE 

C 

R.E 

E 

K. 

M 

1C 

HIG 

AN. 

U. 

S. 

A.  ^    \ 

Fig.  190.      Multistage  Volute  Pump 
with  Hydraulic  Balancing  Device. 

Single  and  Double  Suction  Pumps 

Centrifugal  pumps  may -also  be  classified  into  single  and 
double  suction  according  to  whether  the  impeller  takes  the  water 
from  one  or  both  sides.  With  the  single  suction  pump,  there  is 
an  unbalanced  condition  in  the  impeller,  which  creates  an  end 
thrust,  and  provision  is  generally  made  to  take  care  of  this  by 
a  thrust  bearing  of  either  the  hydraulic  type  or  ball  thrust  type. 


Fig.  191.     Double  Suction  Volute  Pump  with  Ball  Thrust  Bearing. 


^?1^ 


95 


;        U 

N 

ION 

STE 

AM 

P 

UM 

P 

C 

OM 

PANY 

3 

Fig.  47.    Double  Suction  Volute  Pump,  Horizontal  Split  Case  Type. 

In  the  double  suction  pump,  the  impeller  takes  the  water 
from  both  sides,  and  is  theoretically  balanced,  but  in  practice 
it  has  been  found  that  owing  to  slight  variations  in  castings 
and  local  conditions,  which  exist,  this  type  of  impeller  is  not 
always  balanced,  and  it  is  advisable  to  provide  a  thrust  bearing 
which  is  generally  of  the  ball  type. 


Fig.  48.    Single  Suction  Impeller. 


Fig.  49.    Impeller  of  Double  Suction  Pump. 


Fig.  50.     Ball  Thrust  Bearing. 


|         PUMPING 

MACHINERY, 

AIR   COMPRESSORS 

96 


c 

BATTLE 

C  REEK. 

MICHIGAN. 

U. 

S-'A3 

Advantages  of  Centrifugal  Pumps 

The  chief  advantages  of  the  centrifugal  pump  over  other 
types  of  pumps  are  its  simplicity,  reliability  and  ease  of  opera- 
tion. 

Another  important  feature  is  that  the  discharge  is  smooth 
and  continuous,  and  free  from  shocks  and  pulsations.  Since 
the  centrifugal  pump  is  free  from  vibration,  it  does  not  require 
an  elaborate  foundation. 

The  centrifugal  pump  possessing  the  merits  of  high  speed, 
occupies  less  space,  is  lighter  in  weight,  and  generally  costs  less 
than  other  types  of  pumps. 

The  fact  that  the  discharge  from  a  centrifugal  pump  may 
be  shut  off  by  merely  closing  a  valve  in  the  discharge  pipe  with- 
out dangerous  pressures  being  introduced,  or  requiring  the 
motor  to  be  shut  down,  is  another  great  advantage. 


Uses  of  Centrifugal  Pumps 

The  centrifugal  pump  has  reached  such  a  stage  of  develop- 
ment, that  it  is  being  used  in  almost  every  conceivable  industry 
in  which  the  use  of  water  and  other  liquids  play  a  part. 

The  following  brief  outline  will  give  an  idea  of  its  extensive 
use: 

In  the  Brewery 

(Near- Beer) 

In  breweries  and  distilleries,  the  centrifugal  pump  is  suc- 
cessfully employed  in  handling  hot  and  cold  mash,  beer,  grain, 
and  for  circulating  water. 

In  Refrigerating  Plants 

As  a  brine  pump  in  refrigerating  plants,  the  centrifugal 
pump  is  a  success  on  account  of  its  constant  discharge  pressure. 

In  the  Chemical  Industry 

In  the  chemical  industry,  in  soap  and  oil  plants,  liquids 
are  handled  by  centrifugals. 


AND    CONDENSERS    FOR   EVERY  SERVICE 


For  Drainage  and  Irrigation 

Drainage  and  Irrigation  pumps  usually  involve  low  heads 
and  generally  the  amount  of  power  to  be  supplied  is  compara- 
tively small.  The  centrifugal  pump  for  this  service  is  a  desir- 
able unit  on  account  of  its  simplicity,  low  first  cost,  and  low 
operating  expense. 

Elevator  Service 

For  elevator  service,  which  involves  a  supply  of  varying 
quantities  of  water  under  a  high  and  practically  constant  head, 
the  centrifugal  pump  is  particularly  adapted. 

Fire  Pump  Service 

As  a  fire  pump,  the  centrifugal  is  used  extensively  on  ac- 
count of  its  exceptional  reliability  and  simplicity. 

The  power-limiting  characteristic  is  particularly  valuable 
since  it  protects  the  driving  motor  against  overloads;  also  the 
flat  head  delivery  characteristic  will  prevent  excessive  rise  in 
pressure  and  possible  rupture  of  hose,  when  the  delivery  is  de- 
minished. 


Hot  Water  Service 

For  the  circulation  of  hot  water  in  heating  systems,  the 
centrifugal  pump  is  extensively  used  on  account  of  its  constant 
discharge  pressure,  and  because  it  does  not  give  rise  to  disturbing 
noises  in  the  piping  system  and  radiators. 

In  the  House  and  Office  Building 

The  centrifugal  pump  is  particularly  adapted  for  house  and 
office  buildings  where  noiseless  operation  is  imperative,  and  con- 
stant pressure  is  desired. 

In  the  Iron  and  Steel  Industry 

In  the  iron  and  steel  industry,  centrifugal  pumps  have  be- 
come an  important  factor  for  handling  liquids. 


PUMPING    MACHINERY    AIR    COMPRESSORS 


L 

B 

ATTLE 

C 

REE 

K. 

M 

ICH 

IGAN. 

U. 

s. 

A.        fi 

For  Marine  Work 

On  board  ship  for  circulating,  ballast,  general  service,  con- 
densate  and  boiler  feeding,  the  centrifugal  pump  is  being  used 
extensively. 

For  Mine  Service 

Centrifugal  pumps  are  used  in  mining  work  as  station 
pumps,  sinking  pumps,  and  for  sluicing  and  hydraulic  mining. 
They  are  admirably  adapted  for  mine  service,  as  they  require 
little  or  no  foundation,  do  not  produce  vibration  in  the  pipe 
line,  involve  little  cost  for  installation,  and  when  electrically 
operated,  are  easily  controlled  from  a  distant  point. 

In  the  Oil  Industry 

Centrifugal  pumps  are  being  used  extensively  in  the  oil 
industry  for  handling  oils  where  the  viscosity  is  such  that  it 
is  possible.  This  type  of  pump  is  particularly  adapted  for 
handling  light  oils  such  as  light  crudes,  gas  oil,  kerosene,  gaso- 
line, etc. 

Paper  Mills 

In  the  paper  mill,  the  centrifugal  pump  is  used  extensively 
for  circulating  water,  handling  pulp,  etc. 

The  open  impeller  pumps  are  particularly  adapted  for  hand- 
ling liquids  containing  solid  matter. 

In  the  Power  House 

In  power  nouse  work,  centrifugal  pumps  are  used  for  boiler 
feeding,  condensate  pumps,  circulating  pumps  with  surface,  jet 
and  barometric  condensers,  sump  pumps,  etc. 

For  the  Sugar  House 

In  sugar  houses  and  refineries,  where  reliability  is  the  chief 
requirement,  centrifugal  pumps  are  used  extensively  for  water 
supply,  juices,  carbonation  pumps,  filter  press  pumps,  etc. 

Water  Works  Service 

For  water  works  service,  centrifugal  pumps  are  used  for  the 
main  pumping  units,  for  booster  pumps,  and  in  connection  with 
filter  plants,  for  filling  sedimentation  basins,  flushing  filters,  etc. 


99 


3 


Data  Required  for  Estimates  for  Union 
Centrifugal  Pumps 

When   sending  for  estimates,  please  answer  the  following 
questions : — 

1.  Number    of   pumps   required •„'. 

2.  Capacity  of  each  pump... U.  S.  gallons  per  minute. 

3.  Total  lift,  including  suction  lift,  discharge  lift,  and  pipe 
friction feet. 

4.  Length and  size of  suction  pipe 

and  maximum  distance  from  water  level  to  pump feet. 

5.  Length and    size of    discharge 

pipe,  number and  type of  elbows  and 

bends. 

6.  Nature  of  liquid  to  be  handled ..Fresh  water, 

salt  water,  acidulous,  alkaline,  gritty,  solids  in  suspension? 

7.  Temperature  of  liquid °  Fah.  Specific  gravity 


8.  Service,  continuous Intermittent 

9.  If  electric-motor-driven,  state  characteristics  of  current 

If  direct   current,   give   voltage If  alternating 

current,    give    voltage cycles phase 

10.  If  steam  driven,  state  whether  connected  to  steam  tur- 
bine or  steam  engine. 

11.  Give  steam  pressure,  superheat,  if  any,  and  state  whether 
condensing  or  non-condensing. 

12.  If   belt  driven,   give   dimensions   and   speed   of   driving 
pulley. 

NOTE. — Give  additional  information  as    to   location,  service  of   pump,  special  con- 
ditions, etc.,  in  order  to  enable  us  to  furnish  the  proper  outfit. 


100 


BATTLE      C 


Fig.  51. 

Impeller  Diagram 

In  the  above  diagram 

V2=  Tangential  velocity,  impeller  at  outer  periphery. 

Vj=  Tangential  velocity,  impeller  at  inner  periphery. 

Z2  =  Relative  velocity  of  water  at  outlet. 

Z1=  Relative  velocity  of  water  at  inlet. 

C2  =  Absolute  velocity  of  water  at  outlet. 

J2  =  Radial  velocity  of  water  at  outlet. 

J1  =  Radial  velocity  of  water  at  inlet. 

W  = Tangential  velocity  of  water  at  outlet. 

a2  —  Outlet  angle  of  impeller. 

at  =  Inlet  angle  of  impeller. 

The  above  diagram  illustrates  the  layout  of  a  centrifugal 
pump  impeller.  Like  all  engineering  work,  the  various  factors 
entering  into  the  design  of  centrifugal  impellers  are  determined 
by  experience.  The  design  of  a  centrifugal  pump  impeller  is 
ultimately  based  on  the  performances  of  other  impellers.  The 
theory  indicates  what  would  be  the  general  effect  of  altering 
certain  dimensions,  hence,  successful  design  consists  of  modify- 
ing or  changing  the  design  of  impellers,  which  have  been  tested 
out. 


AND    CONDENSERS    FOR    EVERY  SERVICE 


Theory 

Referring  to  figure  51,  the  water  enters  the  impeller  inlet 
with  a  radial  velocity  Jlf  and  leaves  the  impeller  with  an  absolute 
velocity  of  C2.  The  inner  peripheral  velocity  of  the  impeller 
is  Vlf  and  the  outer  peripheral  velocity  V2.  All  velocities  are  in 
feet  per  second.  ' 

Let  H  be  the  theoretical  head  in  feet  against  which  the 
pump  would  deliver  water,  if  there  were  no  losses.  Then 


V| 
T 

2g 


(21) 


In  which  g  =  the  force  of  attraction   of  gravity  =32. 2  ft. 
per  second. 

From  formula  21 


Having  given  the  head  against  which  the  pump  must  work 
and  the  diameter  of  the  impeller,  the  speed  of  the  pump  may  be 
calculated  by  formula  21. 

EXAMPLE:  Assume  we  have  to  pump  against  a  head  of 
100  ft,,  and  have  an  impeller  of  W%ff  diameter.  What  would 
be  the  required  speed  of  the  pump  ? 

By  substituting  in  formula  21,  we  have: 


V2=V2gH 


V2  =  V2  x  32.2  x  100  =80.4  ft.  per  second. 

This  is  equal  to  80.4  x  60=4824  ft.  per  minute. 

The  circumference  of  the  impeller  10^"  in  diameter  = 
10#  x  3.14  =33.8*  or  2.8  ft. 

As  the  impeller  has  to  revolve  4824  ft.  per  minute,  it  will 
have  to  run  fj-  =  1722  revolutions  per  minute. 

The  capacity  of  a  pump  depends  upon  the  size  of  the  suc- 
tion and  discharge  openings,  the  size  of  the  casing,  and  width 
and  diameter  of  the  impeller.  These  factors  are  determined 
by  the  designer  from  experience. 


102 


*  s^y*- 

***•*•*>•?. 

R 

"A 

T  f  L  E 

C 

REE 

K. 

MICHIGAN, 

U. 

s. 

A 

-J 

Belt-Driven  Pump.     Fig.  192. 


Union    Belt-Driven    Side-Suction  Volute   Pumps 

Maximum  Working  Pressure  52  pounds,  or  120  feet. 


Pipe  Sizes 

Capacity,  G.  P.  M. 

Standard 
Pulleys 

SIZE 

~ 

OF 

B 

PUMP 

Discharge 
Inches 

Suction 
Inches 

Minimum 

Normal 

Maximum 

|l 

jf 

H 

H 

1 

5 

12 

16 

3 

2 

1  /^ 

10 

25 

35 

3 

3 

\\^ 

1/4 

iH 

25 

60 

90 

4 

4 

i/^ 

1  V£ 

2 

40 

90 

125 

5 

5 

2 

2 

3 

75 

200 

260 

6 

6 

2/^j 

2//£ 

3 

125 

260 

300 

6 

6 

3 

3 

4 

200 

400 

600 

8 

6 

4 

4 

5 

300 

500 

700 

8 

8 

5 

5 

6 

400 

800 

1000 

10 

8 

6 

6 

8 

500 

1000 

1200 

10 

10 

8 

8 

10 

1200 

1500 

2000 

12 

12 

10 

10 

12 

1500 

3000 

3500 

14 

12 

12 

12 

14 

2500 

4000 

5000 

16 

14 

AND    CONDENSERS    FOR    EVERY  SERVICE 


103 


Motor-Driven  Pump.     Fig.  193. 


Union  Motor-Driven  Side-Suction 
Volute  Pumps 

Maximum  working  pressure  52  pounds,  or  120  feet. 


Pipe  Sizes 

Capacity,  G.  P.  M. 

SIZE 
OF 

PUMP 

Discharge, 
Inches 

Suction, 
Inches 

Minimum 

Normal 

Maximum 

% 

H 

1 

5 

12 

16 

i 

1M 

10 

25 

35 

iU 

IK 

m 

25 

60 

90 

ilA 

IH 

2 

40 

90 

125 

2 

2 

3 

75 

200 

260 

2y2 

2^ 

3 

125 

260 

300 

3 

3 

4 

200 

400 

600 

4 

4 

5 

300 

500 

700 

5 

5 

6 

400 

800 

1000 

6 

6 

8 

500 

1000 

1200 

8 

8 

10 

1200 

1500 

2000 

10                10 

12 

1500 

3000 

3500 

12         II       12 

14 

2500 

4000 

5000 

104 


1 

a3j 


C  R-EEK •• 


Belt  Driven  Pump.     Fig.  54. 


Motor  Driven  Pump.     Fig.  55. 


Union  Horizontal  Double-Suction  Volute  Pumps 
Horizontal  Split-Case  Type 


Pipe  Sizes 

CAPACITY,  G.  P.  M. 

Standard 
Pulleys 

SIZE 

£, 

OF 

Bl 

PUMP 

5 

8 

6 

*3 

h 

l| 

I"  Z 

Ji 

| 

'rt 
g 

O 

| 

1o    to 
|| 

II 

11A  BL 

iy2 

2 

100 

40 

90 

125 

5 

5 

2BS 

2 

3 

100 

75 

125 

150 

5 

5 

2  BL 

2 

3 

150 

75 

125 

150 

5 

5 

3BS 

3 

4 

100 

175 

280 

325 

6 

6 

3BL 

3 

4 

200 

175 

280 

325 

6 

6 

4BS 

4 

5 

100 

300 

450 

600 

8 

8 

4BL 

4 

5 

203 

300 

450 

600 

8 

8 

5BS 

5 

6 

100 

450 

800 

950 

10 

10 

5BL 

5 

6 

200 

450 

830    ' 

950 

10 

10 

6BS 

6 

8 

103 

600 

1000 

1400 

10 

10 

6BL 

6 

8 

200 

600 

1000 

1400 

10 

10 

8BS 

8 

10 

100 

1000 

2000 

2300 

12 

12 

8BL 

8 

10 

200 

1000 

2000 

2300 

12 

12 

10  BS 

10 

12 

100 

1600 

3000 

4000 

14 

12 

10  BL 

10 

12 

200 

1600 

3000 

4000 

14 

12 

12  BL 

12 

14 

200 

2800 

4000 

5000 

15 

12 

14.BL 

14 

16 

200 

3500 

5500 

6500 

16 

It 

105 


]l        UN 

I  ON 

STEAM 

P  UMP 

COMPANY     ^ 

Motor-Driven  Pump.     Fig.  194. 


Union  Double-Suction  Volute  Pumps 

High  Speed. 

For  Maximum  Heads  of  250  feet  at  3500  R.  P.  M.,  also  for  Low  Heads 

at  1750  R.  P.  M. 


PIPE  SIZES 

CAPACITY,  G.  P.  M. 

SIZE  OF 
PUMP 

Discharge, 
Inches 

Suction, 
Inches 

Minimum 

Normal 

Maximum 

2 

2 

3 

100 

200 

300 

3 

3 

4 

200 

400 

500 

4 

4 

5 

300 

500 

750 

5 

5 

6 

500 

800 

1000 

6 

6 

8 

800 

1200 

1400 

[ACHINERY,    AIR   COMPRESSORS 


106 


Fig.  195.     Belt-Driven  Pump. 


Fig.  196.     Motor-Driven  Pump. 


Union  Multistage  Centrifugal  Pumps 


- 

PIPE  SIZES. 

CAPACITY,  G.  P.  M. 

SIZE  OF 
PUMP 

Discharge, 
Inches 

Suction, 
Inches 

Minimum 

Maximum 

V4 

11A 

2 

40 

120 

*2HS 

2 

3 

.50 

100 

2 

2 

3 

50 

175 

3 

3 

4 

150 

350 

4 

4 

5 

300 

650 

5 

5 

6 

450 

900 

6 

6 

6 

600 

• 

1200 

''This  size  only  has  ball-bearings. 


AND    CONDENSERS    FOR   EVERY"  SERVICE 


107 


Fig.  179. 


Union  Motor-Driven  Automatic  Centrifugal 
Pumps  and  Receivers 


Size  Pump 
Discharge 

**Radiation 
(Direct) 
Surface 
Sq.  Feet 

2 
p; 
6 

Max.  Disch. 
ft  Pressure 

R.  P.  M.* 

ti 

i-O 

*g 
K2 

Receiver 
Dimensions 
(Inside) 

Lbs- 

Feet 
Head 

Min. 

Max. 

Dia. 

Height 

H 

% 
3A 

5000-7500 
5000-7500 
5000-7500 

15 
15 
15 

5 
10 
15 

11.5 
13 
34.5 

11.5 
23 
34.5 
46 

1200 
1700 
2000 

1700 
2000 
2500 

X 

1A 
3A 

15 
15 
15 

to  to  to  to  I  to  to  to 

i 
l 
l 
l 

IX 
IX 
IX 
IX 
tX 
IX 

7500-12000 
7500-12000 
7500-12000 
7500-12000 

24 
24 
24 
24 

5 
10 
15 
20 

1100 
1300 
1600 
1750 

1100 
1150 
1350 
1500 
1700 
1800 

1700 
1700 
2000 
2500 

1700 
1700 
1700 
1700 
2000 
2000 

1A 

y± 
i 

15 
15 
15 
15 

12000-30000 
12000-30000 
12000-30000 
12000-30000 
12000-30000 
12000-30000 

60 
60 
60 
60 
60 
60 

5 
10 
15 
20 
25 
30 

11.5 
23 
34.5 
46 
57.5 
69 

*A 
i 

ilA 

3 
3 
3 

22 
22 
1  22 
22 
22 
22 

36 
36 
36 
36 
36 
36 

m 

11A 
llA 
11A 
llA 
11A 
llA 

30000-40000 
30000-40000 
30000-40000 
30000-40000 
30000-40000 
30000-40000 
30000-40000 

80 
80 
80 
80 
80 
80 
80 

5 
10 
15 
20 
25 
30 
35 

11.5 
23 
34.5 
46 
57.5 
69 
81 

1100 
1100 
1100 
1100 
1300- 
1400 
1500 

1400 
1700 
1700 
1700 
1700 
1700 
1700 

IJ4 

m 

2 
3 
5 
5 
5 

22 
22 
22 
22 
22 
22 
22 

36 
36 
36 
36 
36 
36 
36 

*RPM  refers  to  the  full-load  speed  of  the  motor. 

**For  indirect  radiation  as  in  fan  system,  one-fifth  of  the  ratings  given  should  be  used. 

tUse  motors  of  40°  Centrigrade  rating. 

ttln  figuring  total  head,  allow  5  Ibs.  margin  for  forcing  water  into  the  boiler. 

For  higher  pressure,  special  pumps  can  be  furnished  upon  request. 


L 

B 

ATTLE 

C 

REE 

K. 

MIC 

HIGAN, 

U. 

s. 

A.        jj 

Fig.  180.    Single  Sump  Pump.  Fig.  197.     Duplex  Sump  Pump. 

Union  Vertical  Sump  Pumps 

Single  and  Duplex. 


SIZE 
PUMP 

Size  Discharge 

Diameter  of 
Cpver  in  Inches 
Single 

Diameter  of 
Cover  in  Inches 
Duplex 

J  Depth  of 
Pit  in  Feet 

**1 

1 

30 

48 

6 

1M 

1M 

36 

60 

6 

lj^ 

i/^ 

42 

60 

6 

2 

2 

42 

60 

6 

2/^ 

2//£ 

48 

68 

6 

3 

3 

48 

68 

6 

4 

4 

52 

68 

6 

**This  pump  is  not  suitable  for  handling  soil. 

JFor  pits  deeper  than  6  feet,  steady  bearings  are  used. 

Capacity,  Speed  and  Horse  Power  Table  for  Vertical  Sump  Pumps 

HEAD  IN  FEET 


10 

20 

30 

40 

50 

* 

P, 

a 

p. 

a 

P. 

s 

a 

s 

P. 

a 

Pi 

Pi 

PH  H-> 

«  6 

pi 

PH  -2 

<D    B 

PH 

Pi  -S 

<u  E 

'  PH 

PU    -M 

<u  S 

pi 

pi  2 

6 

£cS 

pi 

££ 

N     £ 

pi 

«l 

</2  P< 

C* 

ffiS 

II 

Pi 

ffi£ 

tO  OH 

P< 

WS 

10 

1 

1150 

~x 

1 

1740 

K 

1 

1740 

~~% 

1 

1740 

1 

1M 

1740 

IK 

20 

1 

1150 

X 

1 

1740 

3/ 
/4 

1 

1740 

M 

1 

1740 

1 

1M 

1750 

2 

30 

1 

1150 

K 

1 

1740 

1 

1740 

1 

1 

1740 

IK 

1M 

1750 

2 

40 

1  /4 

1150 

K 

IX 

1150 

1    4 

IX 

1740 

IK 

IX 

1740 

2 

1  M 

1750 

2 

50 

1/4 

1550 

X 

1150 

1 

1740 

IK 

IX 

1750 

2 

i  M 

1750 

3 

75 

IK 

1150 

i  K 

1150 

1  K 

1  J4 

1750 

2 

IX 

1750 

3 

i  /4 

1750 

3 

100 

1150 

IK 

IK 

1150 

IK 

IK 

1150 

3 

IK 

1750 

5 

IK 

1750 

5 

150 

2 

1150 

IK 

2 

1150 

2 

2 

1150 

3 

2 

1150 

5 

2 

1750 

5 

200 

2 

1150 

IK 

2 

1150 

3 

2 

1150 

3 

2 

1150 

5 

2 

1750 

7K 

250 

2K 

1150 

2 

2K 

1150 

3 

2K 

1150 

5 

2K 

1150 

5 

2 

1750 

7K 

300 

3 

1150 

2 

3 

1150 

5 

K 

1150 

5 

2K 

1150 

7K 

3 

1150 

7K 

350 

3 

1150 

2 

3 

1150 

5 

3 

1150 

5 

3 

1150 

7K 

3 

1150 

10 

400 

3 

1150 

3 

3 

1150 

5 

3 

1150 

7K 

3 

1150 

7K 

4 

1150 

10 

500 

4 

860 

3 

4 

1150 

5 

4 

1150 

7K 

4 

1150 

10 

4 

1150 

15 

600 

4 

860 

5 

4 

1150 

7K 

4 

1150 

10 

4 

1150 

10 

4 

1150 

15 

AND    CONDENSERS    FOR   EVERV  SERVICE 


107B 


STEAM       PUMP       COMPANY 


Fig.  186. 


Union  Two-Stage  House  Pump 


G.  P.  M. 

10 

15         20 

25 

30 

35 

40 

45 

50 

Speed,  Max. 
Min.  R.  P.  M. 

Pounds  Pressure  or  Foot  Elevation  and  H.  P. 
of  Motor  Required 

Max.   3600 
Min.    3400 

Pressure 
Elevation 

78 
180 

71.5 
165 

65 
150 

61.5 
142 

50 
115 

Motor  H.P. 

| 

5 

5 

5 

5 

5 

Max.  3600 
Min.    3200 

Pressure 
Elevation 

i 
[ 

72.5 
167 

68     |60.5 
157  J140 

54 
125 

47.5 
110 

Motor  H.P. 

3 

3 

3 

3 

3 

Max.  3600 
Min.    3000 

Pressure 
Elevation 

63 
145 

58.5 
135 

52 
120 

45.5 
105 

39 
90 



Motor  H.P. 

3 

3 

3 

3 

3 

Max.  3400 
Min.    2800 

Pressure 
Elevation 

56 
130 

52.5 
121 

47.7 
110 

42 
97 

36 

83 

Motor  H.P. 

2 

2 

2 

2 

0 

27 
62 

Max.  3400 
Min.    2600 

Pressure 
Elevation 

47.7 
110 

43.3 
100 

39 
90 

32.5 
75 



Motor  H.P. 

2 

2 

2 

2 

2 

Max.  3000 
Min.    2400 

Pressure 
Elevation 

41 
95 

39 
90 

34.7 
80 

30.3 
70 

26 
60 

IK 

Motor  H.P. 

IK 

IK 

IK 

IK 

Max.  2800 
Min.    2200 

Pressure 
Elevation 

34.6 

80 

32.5 
75 

27 
62 

24 
55 

IK 

Motor  H.P. 

1 

1 

1 

1 

Max.  2500 
Min.    2000 

Pressure 
Elevation 

27 
63 

26 
60 

21.6 
50 

:  — 

Motor  H.P. 

1 

1 

1 

Max.   2500 
Min.    1700 

Pressure 
Elevation 

21.6 
50 

19.5 
45 

16.5 
38 



—  - 

Motor  H.P. 

K 

K 

2A 

PUMP  ING    MA  C' H"I  NE^^S^EoSFiSSoR  S      Z| 

>••*•»•»«•«•»  fvrfvTnrTr^irv  » ~a • »  w  a  « i^A^jtKJOCOCgxicl^^gJOLJtJLa-TrgY-g  a  w  it  B  »  tf  arBTEg3LJi.a  i-meaaaj 


107  C 


Fig.  198. 
Belt -Driven  Pump. 


Fig.  199. 
Motor-Driven  Pump. 


Union  Centrifugal  Paper  Stock  Pumps 


PIPE  SIZES 

*APPROXIMATE 
CAPACITY,  G.  P.  M. 

Standard 
Pulleys 

SIZE  OP 

PUMP 

Discharge, 
Inches 

Suction, 
Inches 

Minimum 

Maximum 

II 

r| 

P  £ 

fo  J5 

3 

3 

5 

150 

350 

8 

6 

4 

4 

6 

250 

700 

10 

8 

5 

5 

8 

400 

900 

12 

8 

6 

6 

10 

600 

1200 

12 

10 

8 

8 

12 

900 

2000 

14 

12 

*Capacity  will  vary  with  the  consistency  of  stock. 


AND    CONDENSERS    FOR    EVERV  SERVICE 


UNION       STEAM       PUMP       COMPANY 


How  to  Determine  the  Total  Head  of  a 
Centrifugal  Pump 

The  total  head  against  which  a  centrifugal  pump  operates 
is  made  up  of  the  sum  of  four  factors  as  follows:  suction  lift, 
discharge  head,  friction  head  (due  to  loss  in  suction  and  dis- 
charge line) ,  and  velocity  head. 

The  suction  lift  is  the  vertical  distance  from  the  level  of 
the  water  to  be  pumped  to  the  center  line  of  the  pump.  If  the 
water  level  is  above  the  center  line  of  pump,  the  pump  is  operat- 
ing under  a  suction  head  or  a  flooded  suction,  and  this  distance 
must  be  subtracted  from  the  sum  of  the  remaining  factors. 
The  discharge  head  is  the  vertical  distance  between  the  center 
line  of  the  pump  and  the  level  to  which  the  water  is  elevated. 
The  friction  head  for  pipes  and  elbows  for  different  sizes  and 
capacities  can  be  found  on  pages,  144—147. 

The  velocity  head  "H"  is  determined  by  the  Formula 


in  which 


64.4 
v  __  .408  x  Gallons  per  minute 

~1?~" 

D=  Diameter  of  the  pipe  in  inches. 


(22) 


Rig.  61. 

Figure  61,  illustrates  the  proper  method  of  connecting  up 
a  centrifugal  pump  for  testing  purposes. 

Connection  for  suction  gauge  should  be  made  at  least  2>£  " 
from  the  face  of  the  suction  flange  on  pump.  Connection  for 


108 


discharge  gauge  should  be  made  at  least  2>£"  from  the  face  of 
the  discharge  flange  on  the  pump.  All  gauge  connections  should 
be  made  absolutely  tight  and  as  short  as  possible. 

To  arrive  at  the  total  head  that  the  centrifugal  pump 
works  against,  from  the  gauge  readings,  the  following  example 
may  be  used: 

Assuming  the  distance  "A"  (vertical  distance  from  the  center 
line  of  the  gauge  connection  in  suction  pipe  to  center  line  of 
pressure  gauge)  to  be  2  feet,  discharge  pressure  40  pounds 
(by  gauge),  and  vacuum  (by  gauge)  15  inches,  when  discharging 
1,000  gallons  of  water  per  minute.  Let  6  inches  be  the  diameter 
of  the  discharge  pipe  (where  gauge  connection  is  made)  and  8 
inches  be  the  diameter  of  the  suction  pipe  (where  gauge  connec- 
tion is  made).  The  total  head  for  the  above  example  is  arrived 
at  as  follows: 

40  pounds  pressure  (see  page  142)   =92.4     feet. 

15  inches  vacuum  (see  page  152)      =17.01  feet. 

Distance  A  =  2.0 

*Velocity  head  =   1.36. 


Total  head 


=  112.77  feet. 


*The  velocity  head  in  the  6  inch  discharge  pipe  by  formula  (22)  equals  1.99  feet. 
The  velocity  head  in  the  8  inch  suction  pipe  by  formula  (22)  equals  .63  feet.  The  total 
velocity  head  to  be  added,  therefore  equals  the  difference  between  these  two  figures  or 
1.36  feet. 

If  the  suction  and  discharge  pipes  are  of  the  same  diameter 
where  the  gauge  connections  are  made,  the  velocity  head  will 
be  the  same  in  both,  and  no  correction  need  be  made  for  same, 
as  the  suction  gauge  readings  include  the  velocity  head  in  the 
suction  pipe,  which  in  this  instance  is  the  same  as  the  velocity 
head  on  the  discharge  pipe.  Where  the  discharge  pipe  is  smaller 
in  diameter  than  the  suction  pipe,  the  difference  between  the 
velocity  heads  in  both  pipes  should  be  added  to  the  other  read- 
ings given  above  in  order  to  arrive  at  the  total  head.  The 
difference  in  velocity  heads  in  the  suction  and  discharge  pipes 
should  be  subtracted  from  the  sum  of  the  other  readings  given 
above,  if  the  suction  pipe  is  smaller  than  the  disharge  pipe 
where  the  gauges  are  connected.  In  the  above  example,  the 
friction  head  in  the  suction  and  discharge  pipes  is  included  in 
the  gauge  readings. 

It  is  of  the  greatest  importance  that  the  correct  head  be 
determined,  before  purchasing  a  centrifugal  pump. 


AND    CONDENSERS    FOR    EVERT  SERVICE 


STEAM       PU  M  P       COM  P  ANY         I 

•itiy  ••••••,..••,.»>.,..•....»..«,..» .«^ar.r.-¥-ffWTTif™rg* 


By  referring  to  the  characteristics  reproduced  on  page  117, 
it  is  seen  that  should  the  head  be  greater  than  that  for  which 
the  pump  is  designed,  less  water  would  be  discharged,  and  if 
the  head  is  less,  more  water  will  be  discharged.  Particularly  on 
direct  connected  units,  any  error  in  specifying  the  correct  head 
involves  either  changing  the  impeller,  the  prime  mover,  or  both. 

Great  care  should  be  used  in  estimating  the  friction  loss  in 
the  piping,  as  this  may  be  a  very  important -factor  of  the  total 
head. 


Measurement  of  Water 

To  determine  the  volume  of  discharge  of  a  centrifugal  pump 
or  any  pump,  the  means  that  may  be  employed  according  to 
the  circumstances  are  to  weigh  or  measure  the  volume  of  liquid 
discharged  in  a  known  time  interval,  by  using  the  weir,  a  Venturi 
meter,  a  Pitot  tube,  or  a  calibrated  nozzle. 

To  measure  the  volume  of,  or  weigh  the  liquid  discharged 
in  a  certain  time  interval,  is  the  most  accurate  method,  owing 
to  the  fact  that  no  arbitrary  constants  are  necessary  in  calcula- 
tion. 

This  method  of  measurement  is  very  often  used  in  labora- 
tories and  is  the  one  used  in  testing  out  Union  centrifugal  pumps. 

The  Union  Steam  Pump  test  laboratory  is  equipped  with  a 
large  testing  tank  containing  approximately  60,000  gallons  of 
water.  The  pump  takes  the  suction  from  this  tank  and  dis- 
charges it  into  a  smaller  tank  of  exact  known  dimensions. 

The  weir  is  a  standard  device  for  measuring  water.  It 
should  be  remembered,  however,  that  all  weir  formulas  and  co- 
efficients are  purely  empirical  in  their  nature,  and  that  the  dif- 
ferent formulas  that  are  accepted  at  large  do  not  give  identical 
results.  The  most  widely  used  weir  formula  is  the  Francis 
formula  for  rectangular  weirs. 

Q=3.33  (b— .2H)  H*  (23) 

Q=  Cubic  feet  per  second. 

b  =  Breadth  in  feet  of  the  notch  or  length  of  the  weir. 

H  =The  head  in  feet  above  the  crest  measured  by  the 
hook  gauge. 


!^ 

110 


r/t/n/  tv/e*  aox 


O      0     O      0     C     O     0 

0     0     O     O     O     O 

O     O     O     O     O     0     O 
OOOOOOOO 
O     O     O     O     O     O     0 

aoooooon 

O     O     O     O      O     O     O 
OOOOOOOO 
O     O     O     O     0      O     O 
0     O     O      O     O     O      0 
0     O     O     O     O     O     O 

O     O     O     O      O      O 
000000 
O      O     O     O      O     O 
O     O      O     O      o     O 

oVoVoV 
o    o    o    o    o   o 
o    o    o    o    o    o 

l»      0     0     O     O     0 

0     O     0     0     O     O     O 
)     O     O     O     O     O     O 
0     O     O     0     0     O      O 
0     0     O     O     O     O      O 
0     O     O     O      O      O      0 
0     O     O     O     O      O      O 
O     O     O     O     O      O     O 
J     O     O     O      O      O     O 
O     O     O      O      O     O      0 
>     O     O      O      O     O     O 
O     O     O      O      O     0     O 
)     O     O      O      O     O     O 
O      0     O      O     0     O     C 

**      o    o   o    o    o 
o    o    o    o    o 
o    o    o    o    o 

O     O     O     O     O 
0     0     0     0      0 

o    o   o    o    o 
»Vo°oV 

oVoVo0 

0     0      o      00 

°o°o0o0o% 

-d 

Fig.  62. 

Standard  Full  Contracted  Rectangular  Weir  Box 
for  Measurement  of  Water 

Figure  62  illustrates  a  standard  full  contracted  weir  box 
for  the  measurement  of  water. 

In  constructing  the  same,  it  is  necessary  that  the  board 
over  which  the  water  falls,  be  beveled  on  the  down  stream  side; 
the  ends  should  also  be  beveled  on  the  same  side,  leaving  the  edge 
almost  sharp,  say  within  one-eighth  of  an  inch.  The  hook 
gauge  must  first  be  set  at  zero  when  the  point  of  hook  is  level 
with  the  crest  of  weir  by  use  of  a  spirit  level.  Or  it  can  be  set 
perfectly  accurate  with  the  water  level  just  at  the  crest  of  the 
weir  and  point  of  hook  showing  above  the  water. 

The  tables  on  the  following  pages  are  based  on  zero  velocity 
of  approach,  i.  e.,  the  water  should  not  approach  the  weir  with 
any  noticeable  velocity,  as  otherwise  a  greater  quantity  would 
be  discharged  than  indicated  by  the  depth. 

The  length  of  the  weir  should  be  less  than  two-thirds  the 
width  of  the  box,  and  the  depth  of  the  box  should  be  more  than 
three  times  the  depth  of  water  flowing  over  the  crest  of  the  weir. 

Francis  says  a  fall  below  the  crest  of  the  weir  of  one-half 
the  head  is  sufficient,  but  there  must  be  a  free  access  of  air  tinder 
the  sheet.  However,  we  recommend  that  the  fall  below  the 
weir  should  be  greater  than  one-half  the  head. 


111 


Discharge  of  Rectangular  Weir 


HEAD 

LENGTH  OF  WEIR 

Addition  for 
Increase  Length 

Inch 

Feet 

12  inch 

24  inch 

3  ft. 

5  ft. 

8ft. 

12  ft. 

20  ft. 

1  in. 

1  ft. 

& 

0.005 

1 

0.010 

1.48 

0.138 

1.592 

3% 

0.015 

2.915 

0.243 

2.220 

0.021 

4.49 

9. 

13.5 

22.5 

36. 

54. 

90. 

0.374 

4.505 

1*5 

0.026 

6.25 

12.55 

18.8 

31.4 

50.4 

75.6 

126. 

0.526 

6.300 

% 

0.031 

8.24 

16.5 

22.6 

41.25 

66. 

99.5 

165.5 

0.687 

8.282 

1% 

0.036 

10.34 

20.8 

31.2 

52.1 

83.2 

125. 

208.3 

0.868 

10.421 

i 

0.042 

12.64 

25.35 

38.1 

63.4 

101.8 

153. 

255. 

1.062 

12.73 

T% 

0.047 

15.08 

30.3 

45.5 

76.1 

121.5 

182. 

304. 

1.269 

15.20 

0.052 

17.6 

35.4 

53.1 

89.1 

142. 

214. 

356. 

1.485 

17.81 

* 

0.057 

20.3 

40.85 

61.1 

102.8 

164. 

246.5 

410.5 

1.710 

20.57 

O.OG2 

23.1 

46.3 

69.7 

117. 

187.5 

281. 

468. 

1.948 

23.40 

* 

0.068 

26. 

52.6 

78.9 

132. 

210.5 

316.4 

529. 

2.200 

26.42 

0.073 

29.1 

58.5 

88.3 

147. 

235.8 

354. 

590. 

2.460 

29.50 

ll 

0.078 

32  2 

64.8 

97.7 

162.8 

252. 

392. 

655. 

2.730 

32.75 

1 

0.083 

35.4 

71.5 

107.5 

179.8 

288. 

432. 

770. 

3.010 

36.04 

I* 

0.088 

38.8 

78.3 

118. 

197. 

315. 

472. 

789. 

3.290 

39.50 

1  * 

0.094 

42.2 

85. 

128.2 

214.5 

343. 

515. 

860. 

3.583 

43.02 

lA 

0.099 

45.9 

92.2 

139. 

232.5 

372. 

559. 

931. 

3.882 

46.85 

1  i 

0.104 

49.5 

99.8 

150.4 

250.4 

401. 

604.5 

1006. 

4.199 

50.45 

1& 

0.109 

53. 

107. 

161.5 

270. 

432. 

650. 

1085. 

4.520 

54.00 

0.115 

56.75 

114.7 

173. 

289.5 

464. 

695. 

1160. 

4.855 

58.00 

IT? 

0.120 

60.7 

123. 

185. 

309.5 

496. 

745. 

1240. 

5.175 

62.10 

1  i 

0.125 

64.9 

131. 

197. 

329.5 

528. 

794. 

1323. 

5.570 

65.15 

Hi 

0.130 

68.5 

139. 

209. 

350. 

561. 

845. 

1408. 

5.850 

70.10 

1    H 

0.135 

72.5 

147. 

222. 

371.5 

596. 

885. 

1500. 

6.203 

74.70 

Hi 

0.143 

77. 

156. 

235. 

392.6 

630. 

947. 

1580. 

6.570 

79.15 

1 

0.146 

81. 

164. 

248. 

415. 

665. 

1000. 

1680. 

6.985 

83.20 

li 

0.151 

85.4 

173. 

262. 

436.5 

701. 

1053. 

1760. 

7.340 

87.75 

1  1 

0.156 

89.5 

182. 

275. 

460. 

736. 

1109. 

1852. 

7.690 

92.70 

lii 

0.161 

94. 

191. 

289. 

483.5 

775. 

1164. 

1942. 

8.100 

97.20 

2 

0.167 

98.5 

200.5 

302. 

506. 

812. 

1220. 

2040. 

8.515 

102.00 

2A 

0.172 

103. 

210. 

316. 

530. 

850. 

1278. 

2130. 

8.911 

106.80 

2  * 

0.177 

107.8 

219.9 

332. 

555. 

890. 

1330. 

2230. 

9.316 

111.70 

2i% 

0.182 

112.4 

229. 

345. 

579. 

930. 

1397. 

2330. 

9.715 

116.60 

2  * 

0.187 

117. 

239. 

361. 

605. 

970. 

1453. 

2430. 

10.  122 

121.30 

2^ 

0.193 

122. 

249. 

376. 

629. 

1010. 

1518. 

2530. 

10.590 

127.00 

2  j 

0.198 

127. 

259. 

390.5 

655. 

1050. 

1580. 

2637. 

10.990 

132.00 

2^ 

0.203 

132. 

269. 

406. 

680. 

1092. 

1640. 

2738. 

11.420 

137.20 

2J 

0.208 

136.2 

279. 

422. 

706. 

1133. 

1707 

2846. 

11.890 

142.90 

2& 

0.213 

142. 

289. 

438. 

732. 

1176. 

1769. 

2955. 

12.320 

148.00 

2  ^ 

0.219 

146.7 

300. 

453. 

760. 

1220. 

1832. 

3057. 

12.790 

153.50 

% 

0.224 

151.4 

310.5 

470. 

785. 

1265. 

1900. 

3165. 

13.210 

159.00 

2 

0.229 

157. 

321.5 

485. 

815. 

1308. 

1968. 

3275. 

13.590 

164.20 

2* 

0.234 

162. 

332. 

501.5 

832.5 

1352. 

2034. 

3470. 

14.19 

170.15 

2 

0.240 

167.6 

343. 

520. 

870. 

1400. 

2103. 

3500. 

14.61 

175.3 

m 

0.245 

172.9 

354. 

535. 

898. 

1442. 

2171. 

3611. 

15.05 

181.4 

3 

0.250 

177.8 

366. 

552. 

926. 

1490. 

2239. 

3740. 

15.61 

187.3 

0.255 

183.3 

377. 

569. 

956. 

1536. 

2309. 

3853. 

16.1 

193.5 

3*4 

0.260 

189.1 

388. 

588. 

986. 

1580. 

2380. 

3975. 

16.6 

199.2 

0.266 

194.8 

400. 

605. 

1015. 

1632. 

2449. 

4092. 

17.1 

205.5 

3  i 

0.271 

199.8 

410.5 

624. 

1047. 

1679. 

2522. 

4210. 

17.6 

211. 

3& 

0.276 

205.6 

422. 

640. 

1076. 

1728. 

2598. 

4341. 

18.11 

217  6 

8| 

0.281 

210.8 

435. 

659. 

1105. 

1778. 

2671. 

4455. 

18.63 

224. 

3ft 

0.286 

216.5 

446. 

676. 

1138. 

1825. 

2740. 

4575. 

19.11 

229.8 

3  i 

0.292 

222. 

458. 

695. 

1167. 

1875. 

2820. 

4710. 

19.7 

236.  15 

0.297 

228. 

470. 

714. 

1200. 

1925. 

2898. 

4846. 

20.2 

242.2 

3  - 

0.302 

234. 

483. 

731. 

1230. 

1977. 

2970. 

4961. 

20.78 

249.4 

3i 

0.307 

240. 

445. 

750. 

1260. 

2027. 

3043. 

5100. 

21.3 

255.9 

3 

0.312 

245. 

506. 

769. 

1292. 

2081. 

3121. 

5213. 

21.83 

262.2 

3f 

0.318 

251. 

520. 

789. 

1328. 

2128. 

3203. 

5350. 

22.4 

268.6 

3 

0.323 

256.5 

533. 

808. 

1355. 

2180. 

3280. 

5475. 

22.9 

274.5 

3f 

0.328 

263. 

545. 

825. 

1390. 

2239. 

3360. 

5610. 

32.5 

282. 

4 

0.333 

269. 

556. 

846. 

1424. 

2288. 

3440. 

5748. 

24. 

288. 

4^ 

0.338 

275.6 

570. 

866. 

1454. 

2342. 

3520. 

5890. 

24.64 

296. 

0.344 

281.6 

584. 

885. 

1490. 

2399. 

3633. 

6015. 

25.18 

301.9 

M 

0.349 

286. 

596. 

906. 

1523. 

2450. 

3680. 

6150. 

25.78 

309. 

J 

0.354 

293.6 

610. 

925. 

1559. 

2505. 

3775. 

6300. 

26.34 

316. 

'  $ 

0.359 

300. 

623. 

945. 

1590. 

2560. 

3856. 

6425. 

26.94 

323. 

'    j  " 

0.365 

306. 

636. 

966. 

1628. 

2620. 

3935. 

6571. 

27.55 

330.5 

Tl" 

0.370 

312. 

650. 

986. 

1660. 

2670. 

4015. 

6715. 

28.05 

336.8 

I 

0.375 

318. 

663. 

1006. 

1696. 

2704. 

4102. 

6857. 

28.65 

344. 

'I8 

0.380 

325. 

676. 

1030. 

1730. 

2780. 

4195. 

7002. 

29.25 

351.5 

0.385 

331. 

690. 

1050. 

1768. 

2841. 

4275. 

7150. 

29.85. 

358. 

ii 

0.390 

336.6 

704. 

1069. 

1801. 

2899. 

4355. 

7291. 

30.46 

366. 

4 

0.396 

344. 

717.5 

1091. 

1835. 

2958. 

4450. 

7448. 

31.15 

374. 

ft 

0.401 

350. 

731. 

1111. 

1875. 

3010. 

4540. 

7588. 

31.75 

390.9 

4 

0.406 

356.6 

744.5 

1131. 

1908. 

3075. 

4621. 

7710. 

32.36 

388.2 

41 

0.411 

363.7 

759. 

1156. 

1948. 

3132. 

4710. 

7891. 

33. 

395.9 

5 

0.417 

370. 

772. 

1175. 

1985. 

3192. 

4810. 

8039. 

33.65 

404.3 

5^ 

0.422 

376.5 

785. 

1200. 

2018. 

3256. 

4896. 

8172. 

34.2 

410.5 

0.427 

382.5 

800. 

1220. 

2030. 

3313. 

4999. 

8345. 

34.93 

419.4 

5^  * 

0.432 

388. 

815. 

1239. 

2094. 

3368. 

5070. 

8461. 

35.5 

426. 

5    * 

0.437 

395.5 

830. 

1262. 

2130. 

3439. 

5165. 

8643. 

36.  17 

434.4 

£ 

0.443 

401. 

844. 

1285. 

2168. 

3500. 

5255. 

8800. 

36.79 

441. 

112 


Discharge  of  Rectangular  Weir 


HEAD 

LENGTH  OF  WEIR 

Addition  for  In- 
crease of  Length 

Inch 

Feet 

12  Inch 

24  Inch 

3  Ft. 

5  Ft. 

8  Ft. 

12  Ft. 

20  Ft. 

1  Inch 

1  Ft. 

5  I" 

0.448 

409. 

857. 

1310. 

2208. 

3o48. 

5350. 

8949. 

37-.  45 

450. 

5-f-" 

0.453 

415. 

871. 

1330. 

2243. 

3612. 

5446. 

9111. 

38.1 

457  5 

5  i" 

0.458 

421.6 

887. 

1352. 

2282. 

3680. 

5550. 

38.8 

465.  .5 

5&" 

0.463 

428.5 

903. 

1376. 

2321. 

3724. 

5612. 

39.2 

470.9 

5  H" 

0.469 

435.5 

915. 

1395. 

2358. 

3780. 

5710. 

39.98 

480. 

5ii" 

0.474 

442.5 

932.5 

1419. 

2400. 

3842. 

5802. 

9706! 

40.61 

487.6 

5  1" 

0.479 

449. 

947.5 

1442. 

2440. 

3913. 

5899. 

9846 

41.22 

495. 

5H" 

0.484 

456.2 

960. 

1465. 

2480. 

3971. 

5990. 

10000. 

41  95 

503.5 

5  i 

0.490 

462.6 

977. 

1490. 

2514. 

4043. 

»6078. 

10186. 

42.6 

511. 

5H 

0.495 

470. 

993. 

1515. 

2559. 

4105. 

6176. 

10325. 

43.26 

519.6 

6 

0.500 

476.5 

1005. 

1535. 

2600. 

4161. 

6289. 

10510. 

44. 

528. 

0.505 

1021. 

1561. 

2640. 

4230. 

6398. 

10657. 

44.65 

536. 

6  i 

0.510 

1039. 

1582. 

2675. 

4292. 

6490. 

10812. 

45.25 

543 

0.515 

1051. 

1609. 

2716. 

4361. 

6571. 

10996. 

46.10 

554. 

6  i 

0.521 

1068. 

1632. 

2760. 

4423. 

6670. 

11175. 

46.6 

560. 

0.526 

1083. 

1655. 

2801. 

4500. 

6796. 

11321. 

47.5 

570. 

6*i 

0.531 

1100. 

1679. 

2844. 

4558. 

6890. 

11500. 

47.95 

575. 

gi 

0.536 

1112. 

1704. 

2881. 

4641. 

6972. 

11680. 

48.81 

586. 

0  i 

0.542 

1130. 

1742. 

2920. 

4710. 

7062. 

11825. 

49.7 

596. 

6& 

0.547 

1147. 

1752. 

2962. 

4762. 

7189. 

11990. 

50.2 

602.3 

6  i 

0.552 

1161. 

1779. 

3005. 

4830. 

7288. 

12162. 

51.1 

613.8 

0.557 

1178. 

1803. 

3047. 

4900. 

7376. 

12325. 

51.5 

617.8 

6 

0.563 

1193. 

1826. 

3084. 

4957. 

7487. 

12500. 

52.5 

629.9 

0.568 

1210. 

1853. 

3139. 

5041. 

7590. 

12695. 

53.3 

640. 

e'i 

0.573 

1226. 

1878. 

3180. 

5100. 

7691. 

12850. 

53.8 

645.5 

Cii 

0.578 

1240. 

1903. 

3219. 

5181. 

7790. 

13141 

54.6 

65(>. 

7 

0.583 

1258. 

1928. 

3260. 

5230. 

7902. 

13220. 

55.6 

668. 

0.589 

1272. 

1949. 

3300. 

5310. 

8005. 

13400. 

56. 

672.5 

7l| 

0.594 

1290. 

1976. 

3342. 

5395. 

8112. 

13580. 

56.9 

682.5 

'16 

0.599 

1309. 

2000. 

3384. 

5450. 

8221. 

13755. 

57.85 

695. 

7  i 

0.604 

1322. 

2029. 

3436. 

5561. 

8310. 

13931. 

58.47 

701.5 

0.609 

1339. 

2058. 

3480. 

5595. 

8441. 

14110. 

59.10 

710. 

7  i 

0.615 

1356. 

2080. 

3522. 

5661. 

8540. 

14290. 

59.93 

719.6 

7A 

0.620 

1371. 

2105. 

3570. 

5742. 

8641. 

14480. 

60.6 

729. 

7  i 

0.625 

1345. 

2130. 

3609. 

5807. 

8750. 

14640. 

61.4 

736. 

Hi 

0.630 

1408. 

2155. 

3658. 

5885. 

8850. 

14820. 

62.1 

746. 

7  i 

0.635 

1423. 

2179. 

3700. 

5950. 

8980. 

15015. 

62.96 

755. 

0.641 

1439. 

2212. 

3745. 

6019. 

9093. 

15190. 

63.6 

764. 

7  i 

0.646 

1458. 

2238. 

3785. 

6100. 

9185. 

15395. 

64.49 

774. 

n 

0.651 

1471. 

2260. 

3820. 

6168. 

9291. 

15583. 

65.15 

782. 

7  i 

0.656 

1490. 

2286. 

3860. 

6248. 

9419. 

15751. 

66. 

792. 

0.661 

1506. 

2310. 

3903. 

6310. 

9537. 

15921. 

66.9 

803. 

8  l 

0.667 

1522. 

2338. 

3956. 

6400. 

9644. 

16150. 

67.7 

813.5 

0.672 

1541. 

2365. 

4000. 

6481. 

9746. 

16342. 

68.5 

821.5 

81 
• 

0.667 

1555. 

H396. 

4045. 

6540. 

9866. 

16510. 

69.15 

831. 

Sft 

0.682 

1572. 

2419. 

4090. 

6609. 

9970. 

16700. 

70. 

840. 

8  i 

0.688 

1592. 

2442. 

4140. 

3700. 

10095. 

16900. 

70.8 

850. 

0.693 

1601. 

2460. 

4178. 

6757. 

10195. 

17086. 

71.6 

860. 

tj 

0.698 

1618. 

2493. 

4227. 

6845. 

1031*0. 

17271. 

72.55 

871. 

0.703 

1636. 

2516 

4292. 

6925. 

10425. 

17905. 

73.25 

879.6 

o 

0.708 

1652. 

2540. 

4312. 

6995. 

10530. 

17685. 

74.03 

889.7 

0.174 

1670. 

2565. 

4362. 

7061. 

10645. 

17845. 

74.9 

899. 

I^S 

0.719 

1689. 

2595. 

4415. 

7146. 

10780. 

18042. 

75.65 

909. 

ft 

0.724 

1706. 

2623. 

4460. 

7225. 

10900. 

18220. 

76.52 

919. 

8  : 

0.729 

1723. 

2656. 

4511. 

7293. 

11000. 

18460. 

77.35 

929. 

81- 

0.734 

1741. 

2680. 

4552. 

7380. 

11120. 

18651. 

78.28 

940. 

8  ; 

0.740 

1760. 

2705. 

4600. 

7460. 

11250. 

18872 

79. 

949. 

8ti 

0.745 

1777. 

2739. 

4648. 

7545. 

11355. 

19000. 

79.9 

959. 

9 

0.750 

1791. 

2765. 

4699. 

7600. 

11500. 

19206 

80.65 

969.5 

0.755 

1810. 

2792. 

4749. 

7682. 

11600. 

19400. 

81.52 

979. 

9  i 

0.760 

1830. 

2816. 

4799. 

7755. 

11720. 

19620. 

82.9 

995. 

9i% 

0  765 

1848. 

2844. 

4849. 

7850. 

11831. 

19819. 

83.11 

999. 

9  i 

0.771 

1866. 

2876. 

4899. 

7910. 

11940. 

20031. 

84.25 

1011. 

0.776 

1880. 

2900 

4949. 

8000 

12070. 

20225. 

85.05 

1020. 

91! 

0.781 

1898. 

2927. 

4999. 

8080. 

12190. 

20425. 

85.92 

1031. 

9  A 

0.786 

1918. 

2960. 

5049. 

8160. 

12300 

20625. 

86.76 

1041. 

9  \ 

0.792 

1939. 

2985. 

5098. 

8241. 

12430. 

20865. 

87.6 

1051. 

0.797 

1955. 

3017. 

5145. 

8305. 

12570. 

21035. 

88.3 

1060. 

9^ 

0.802 

1971. 

3041. 

5185. 

8396. 

21221. 

89.45 

1072. 

0.807 

1989. 

3073. 

5227. 

8483. 

12806 

21418. 

90.25 

1082. 

91 

0.812 

2006. 

3101. 

5288. 

8564. 

12945'. 

21625. 

91. 

1091. 

0.818 

2025. 

3129. 

5340. 

8635. 

13050. 

21825. 

91.95 

1103. 

9 

0.823 

2045. 

3160. 

5393. 

8710. 

13190. 

22083. 

92.85 

1112. 

91 

0.828 

2065. 

3190. 

5443. 

8800. 

13300. 

22275. 

93.80 

1125. 

10 

0.833 

2085. 

3216. 

5490. 

8892. 

13430. 

22532. 

94.6 

1136. 

EXAMPLE— Suppose  weir  length  is  S  ft.,  and  after  the  water  has  been  flowing  sometime,  the  head  or 
depth  of  flow  is  found  to  be  5  3-16  inches.  To  find  the  number  of  gallons  flowing  per  minute  thru  the  weir,  run 
down  the  "Head"  column  until  5  3-16  inches  is  reached,  then  crosswise  to  the  column  labeled  5  ft.,  and  the  flow 
is  found  to  be  2094  gallons  per  minute. 

If  the  weir  has  a  different  length  than  any  given  in  the  table,  such  as  73  Inches,  'or  5  ft-4-1  ft.  +  1  inch,  proceed 
as  follows: — Taking  the  "  Head"  the  same  as  in  the  preceding  example,  we  find  the  flow  for  5  ft.  equals  2094,  and 
continuing  across  on  the  same  line  to  the  columns  labeled  "Addition  for  increase  of  length,"  we  find  the  flow  tor 
a  73  inch  weir  for  the  given  "Head"  is  2094  plus  4S6  plus  35.5  equals  2555.5  gallons  per  minute. 


113 


• 


UNION       S  T  E  "AM       P  U  M  P 


For  small  rates  of  discharge,  the  triangular  weir  is  better 
than  the  rectangular  weir.  Any  angle  of  notch  may  be  em- 
ployed, but  the  90°  triangular  notch  is  the  one  most  used.  The 
formula  for  the  90°  notch  is : 

Q  =  2.544  R*  (24) 

Q  =  Cubic  feet  per  second. 

H  =  Head  in  feet. 

The  following  table  has  been  computed  from  the  above 
formula : 


Head 
in  ft. 

G.  P.  M. 
discharge 

Head 

in  ft. 

G.  P.  M. 

discharge 

0.25 
0.30 
0.35 
0.40 
0.45 
0.50 
0.55 
0.60 

36 
56.2 
83 
115 
155 
202 
256 
318 

0.65 
0.70 
0.75 
0.80 
0.85 
0.90 
0.95 
1.00 

389 
468 
555 
655 
760 
879 
1000 
1140 

DISCHARGE  * 

5UCT/ON 


TUBE 


Fig.  63. 

The  Venturi  meter  offers  a  satisfactory  method  of  measur- 
ing water,  and  is  very  often  installed  in  pumping  plants  as  it 
permits  of  the  measurement  of  water  without  any  interference 
in  its  flow.  Figure  63  illustrates  the  arrangement  for  testing 
by  the  Venturi  meter. 

Figure  64  illustrates  an  arrangement  for  measuring  the 
quantity  of  discharge  by  means  of  a  Pitot  tube.  The  tube 
measures  the  velocity  head  at  the  orifice  of  the  discharge  nozzle 


PUMPING    MACHINERY,    AIR   COMPRESSORS 


114 


I 


BAT  t  L  E      C  REEK.     MICH  I  G  AN .      U.  S .  A. 


1 


Ul 


SVCT.  GAG£ 


GAT£  VALVE 
5UCT/OA/ 


GflT£  VALV£ 


PfTOT   TUBS 


Fig.  64. 
and  the  quantity  of  discharge  can  be  found  from  the  formula: 

Q=CAV2lH  (25) 

In  which  Q  equals  the  quantity  of  discharge  in  cubic  feet 
per  second,  C  is  a  constant  for  the  nozzle  which  varies  from  .95 
to  .98.  A  equals  the  area  of  the  nozzle  in  square  feet,  H  equals 
the  velocity  head  in  feet. 

The  Pitot  tube  readings  can  only  be  accurate  with  a  care- 
fully calibrated  nozzle  and  a  careful  determination  of  the  co- 
efficient C. 


Fig.  65 

Figure  65  illustrates  a  nozzle  sometimes  employed  in  the 
measurement  of  water.  The  nozzle  used  should  be  carefully 
calibrated,  and  a  curve  of  discharge  plotted,  giving  the  quantity 
of  discharge  from  the  nozzle  for  various  pressures  at  the  point 
where  the  pressure  gauge  is  attached.  The  formula  for  the  dis- 
cbKgei.  '--JT  (28) 


_ 


,)' 


In  which  C  equals  the  coefficient  of  discharge  which  equals 
approximately  .99,  H  is  the  pressure  head  in  the  nozzle  in  feet, 
d  equals  the  diameter  of  the  throat  of  the  nozzle  in  inches,  and  D 
equals  the  diameter  of  the  nozzle  in  inches  at  which  pressure 
is  measured. 


AND    CONDENSERS    FOR    EVERY"  SERVICE 


115 


UNION       STEAM       PUMP       COMPANY 


If  the  pressure  is  measured  in  pounds  per  square  inch,  by  a 
pressure  gauge,  then  H=  2.304  P  +  M 

In  which  P  equals  pressure  in  pounds  per  square  inch  and 
M  equals  the  distance  from  the  center  of  the  nozzle  to  the  pres- 
sure gauge  in  feet.  This  formula  takes  .into  consideration  the 
velocity  of  approach  and  the  water  column  between  the  nozzle 
and  the  gauge. 

Measurement  of  Speed 

To  measure  the  speed  of  a  centrifugal  pump,  the  tacho- 
meter is  the  best  device,  if  it  is  occasionally  calibrated.  A 
revolution  counter  may  also  be  used,  but  care  should  be  ex- 
ercised in  its  use  as  it  does  not  indicate  fluctuations  in  speed, 
and  unless  the  readings  are  extended  over  a  sufficient  period  of 
time,  it  will  not  give  an  average. 

Measurement  of  Power 

The  horse  power  applied  to  the  pump  shaft  may  be  measured 
in  various  ways  depending  upon  the  type  of  prime  mover  em- 
ployed. 

In  testing  laboratories,  centrifugal  pumps  are  tested  by 
means  of  variable  speed,  direct  current  motors.  The  motor 
efficiencies  are  known,  and  by  means  of  Volt  Meters  and  Am- 
meters the  power  input  may  be  accurately  determined  by  the 
formula 

Volts  X  Amperes          ,..          ^^  .  /or7N 

B.  H.  P.  =  -  -  -  -  -  X    Motor  Efficiency        (27) 
746 

The  transmission  dynamometer  is  also  used,  and  is  a  very 
accurate  device.  For  alternating  currents,  the  following 
formula  is  used  for  arriving  at  the  brake  horse  power 

Volts  X  Amperes  X  Cos  0  X  VN  X  M 
r>.  rl.  r.    —  — 


746 

M  =  Motor  Efficiency. 
N  =  Number  of  Phases. 
Cos  $  =  Power  Factor  of  Motor. 

In    the   steam-engine    driven    pump,    the   power   input    is 
arrived  at  by  indicator  cards. 

In    the  gas-engine  driven  unit,  the  power  input  is  measured 
by  the  Prony  brake. 


PUMPING    M  AC  H  fNERY.    AIR   CjOM^R  ES  S  QR^S 

»Wv,«w«.ttVurrffWyuwF«BBiwautfwwwJtt^^ 


116 


Characteristics 


\ 


1 


UOH  . 


D/JJ3 


Characteristics  of  a  5"  Double-Suction  Pump 
Running  at  1700  R.  P.  M.  Constant  Speed. 

Fig.  QQ 


AND    CONDENSERS    FOR    EVERV  SERVICE 


117 


f       UNION 

STEAM 

P  UM  P 

COMPANY     ~J 

On  the  preceding  pages  we  state  how  the  tests  of  centrifugal 
pumps  are  made.  The  results  of  these  measurements  can  be 
produced  graphically  and  the  curves  obtained  illustrate  best 
the  relations  between  capacity,  head,  efficiency  and  brake 
horse  power  (power  input)  of  a  centrifugal  pump  running  at 
constant  speed. 

On  page  117  is  reproduced  a  characteristic  curve- from  an 
actual  test  of  a  5"  double  suction  centrifugal  pump. 

The  variation  in  total  head  corresponding  to  a  variation  in 
capacity  from  zero  to  maximum  is  shown  by  the  curve  marked 
"Head". 

The  power  input  for  different  capacities  is  illustrated  in  the 
curve  marked  "Brake  Horse  Power". 

The  curve  designated  "Efficiency"  shows  the  efficiency  cor- 
responding to  different  capacities. 

The  "Characteristic  curves"  show  that  pumping  against  138 
ft.  total  head,  1020  G.  P.  M.  are  discharged  with  an  efficiency 
of  76  %,  requiring  46.5  H.  P.  to  drive  the  pump.  At  less  capa- 
city, for  instance,  750  G.  P.  M.,  the  pump  will  discharge  against 
155  ft.,  with  74%  efficiency,  with  a  power  input  of  40  H.  P. 

We  see  that  at  1200  G.  P.  M.  the  head  curve  drops  down. 
This  indicates  the  maximum  capacity  of  the  pump.  Inspecting 
the  horse  power  curve  at  the  point  of  maximum  capacity,  we 
note  that  it  also  drops.  Suppose  the  pump  is  sold  for  1020 
G.  P.  M.,  138  ft.  and  46.5  H.  P.  are  required  to  drive  it.  Should 
the  head  drop  to '80  ft.,  the  horse  power  would  decrease  to  39 
horse  power.  An  impeller,  where  the  H.  P.  increases  but 
slightly  or  decreases  after  the  point  of  best  efficiency,  is  called 
"a  non -overload  impeller".  Under  no  circumstances,  in  case 
of  breaking  of  pipes,  valves,  etc.,  can  the  motor  be  seriously 
overloaded.  All  impellers  have  this  desirable  feature,  protect- 
ing the  prime-mover  in  all  cases. 

When  the  discharge  valve  is  entirely  closed,  the  pump  will 
deliver  no  water.  The  head  produced  is  150  ft.  In  actual 
service,  however,  this  head  will  be  greater,  as  the  prime-mover 
works  at  shut-off  of  the  pump  only  under  a  fraction  of  the  rated 
load,  and  electric  motors,  steam  or  water  turbines  run  faster 
at  a  decreased  load,  thus  increasing  the  pressure.  The  "Shut- 
off"  point  therefore  will  be  the  highest  point  on  the  head  curve, 
which  is  of  importance  for  installations  where  there  is  no  friction 
head,  and  pump  has  to  start  against  a  maximum  static  head  from 


the  beginning.  To  rotate  the  impeller  at  this  point,  13  H.  P. 
are  required,  representing  the  friction  of  rotation.  As  no  useful 
work  is  performed  at  the  shut-off  (the  pump  delivering  no  water) , 
the  efficiency  is  zero.  Special  attention  has  to  be  called  to  the 
fact  that  in  contrast  to  a  displacement  pump,  the  head  at  shut- 
off  produced  by  a  centrifugal  pump,  is  from  10  to  20%  greater 
than  the  head  at  maximum  efficiency.  "  No  harm  can  be  don<? 
to  the  pump  or  to  the  pipe  system  by  closing  the  discharge  valves. 

As  long  as  the  water  and  consequently  the  case  do  not  heat 
up  excessively,  due  to  friction  produced  by  the  rotation  of  the 
impeller,  the  centrifugal  pump  may  be  operated  with  a  closed 
discharge  valve. 

Recapitulating,  we  state  the  two  main  points  of  the  charac- 
teristics of  this  pump : 

(1)  The  impeller  gives  high  efficiency  over  a  remarkable 
range  (here  600-1100  G.  P.  M.). 

(2)  A    non-overload    characteristic    protects    the    prime- 
mover  under  all  circumstances  against  serious  overload. 

Different  Types  of  Characteristics 

On  page  120  we  have  reproduced  an  actual  test  of  a  6-inch 
double-suction  centrifugal  pump.  The  efficiency  and  power 
curves  both  show  the  desirable  features  of  the  5-inch  test,  which 
we  described  before;  that  is  good  efficiency  over  a  wide  range 
(here  from  700  to  1200  G.  P.  M.),  and  a  "non-overload"  power 
characteristic. 

By  inspecting  the  "head  curve  "however,  we  note  a  difference : 
the  impeller  of  the  first  pump  produces  a  "flat  characteristic," 
in  other  words,  the  shut-off  point  is  about  5  to  10%  higher 
than  the  point  of  best  efficiency.  The  impeller  in  the  second 
pump  however  produces  a  "steep  characteristic,"  the  shut-off 
being  about  20%  higher  than  the  point  of  best  efficiency. 

In  order  to  decide  which  characteristic  to  use,  various 
points  have  to  be  taken  into  consideration. 

Flat  characteristics  are  suitable  for  installations  where  the 
pump  has  to  maintain  a  constant  pressure  regardless  of  variation 
in  capacity,  as  for  boiler  feeding,  accumulators,  etc. 

Steep  characteristics  are  to  be  used  for  installations  pump- 
ing against  variable  heads,  as  pipe  line  pumps,  or  pumps  where 
the  head  is  purely  composed  of  friction.  In  such  a  case,  a  steep 
characteristic  will  be  safer,  as  should  the  head  vary,  a  pump 


|        AND 

CONDEN 

S 

ERS 

FOR 

EVERY 

5 

ERVICE      "| 

119 


with  a  steep  characteristic  will  adjust  itself  easier  than  a  pump 
with  only  a  small  variation  in  the  head  curve. 

For  every  pump  we  have  a  set  of  different  impellers  to  suit 
the  different  conditions  of  service.  When  ordering,  state  which 
kind  of  characteristic  is  desired,  if  steep  or  flat.  This  will  en- 
able us  to  produce  a  pump  which  will  give  the  best  service. 

Characteristics  of  a  6"  Double-Suction  Pump 

Running  at  1700  R.  P.  M.  Constant  Speed. 


\ 


\ 


\ 


Fig.  67. 


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"~ PUMPING I    MAC HINER.\^_.AIR_COMPRES SjQRS 

...  ^,  ,.  uu  -  ^  w  ^  ^  w  v.  ii^FgwWv/v.  ':--:.., 


120 


1        BATTLE 

C 

REE 

K. 

M 

1C 

HIG 

AN, 

U. 

s. 

A. 

J 

Efficiency  of  Centrifugal  Pumps 

The  efficiency  of  a  centrifugal  pump  is  the  percentage  of 
work  performed  for  the  power  delivered  to  the  pump  shaft, 
and  is  equivalent  to  the  theoretical  horse  power  divided  by  the 
horse  power  applied  to  the  pump  shaft. 

The  efficiency  of  a  centrifugal  pump  varies  according  to 
the  conditions  of  operation,  but  the  following  table  will  give 
a  general  idea  of  the  efficiencies  obtained  in  Union  centrifugal 
pumps. 


SIZE  OF 
PUMP 

Single-Stage 
Single-Suction 
Volute  Pumps 

Single-Stage 

Double-Suction 
Horizontal  Pumps 

Multi-Stage  Pumps 

v± 

20-25 

20-30 

1% 

25-35 

\y> 

25-40 

40-53 

2 

11A 

30-50 
30-52 

40-60 

45-59 

3 

4 
5 
6 
8 
10 
12 

45-56 
50-65 
55-68 
55-70 
65-72 
65-73 
66-75 

48-73 
60-78 
60-80 
65-81 
65-82 
67-83 
68-84 

45-60 
60-67 
63-70 
64-73 
65-76 
68-79 

14 

66-76 

68-85 

Capacity,  Speed,  Head   and   Horse   Power   of 
Centrifugal  Pumps 

In  case  it  is  desired  to  alter  the  capacity,  speed,  or  head 
of  a  centrifugal  pump  in  order  to  suit  some  particular  require- 
ments, it  is  interesting  to  know  that  the  capacity,  speed,  head, 
and  horse  power  bear  the  following  relations  to  each  other. 

Assuming  that  the  quantity  of  water  delivered  by  a  cen- 
trifugal pump  operating  at  N  revolutions  per  minute  is  Q  gallons 
per  minute,  and  the  total  head  the  pump  is  operating  against 
is  H  feet  requiring  P  brake  horse  power  to  operate. 

Now,  if  it  is  desired  to  increase  the  speed  of  this  same  pump 
to  N!  revolutions  per  minute,  this  will  mean  the  pump  will 
now  deliver  Ql  gallons  per  minute,  and  the  total  head  will  be 
H!  feet  requiring  P1  horse  power  to  operate  under  these  con- 
ditions. 

In  order  to  simplify  the  equation,  all  constants  are  eliminated, 
as  the  results  obtained  are  near  enough  for  practical  purposes. 


EVERT  SERVICE 


121 


=  (30)          s  (31) 

t     N,  Ht      (N,)2  Pt      (N,)' 

In  order  to  clearly  illustrate  the  calculation  of  these  form- 
ulae, we  will  assume  that  a  centrifugal  pump  at  its  most  econom- 
ical point  discharges  5000  gallons  per  minute  against  a  total 
head  of  50  feet,  when  operating  at  a  speed  of  900  revolutions 
per  minute,  and  it  requires  90  brake  horse  power.  Now  it  is 
desired  to  increase  this  speed  to  1000  %.  P.  M.  How  much 
water  will  this  pump  discharge  at  its  most  economical  point 
and  what  is  the  total  head  and  horse  power  required  to  operate 
this  pump  under  these  conditions? 

Referring  to  the  above  formulae,  and  substituting  the 
quantities  therein,  we  have 

Q  ....5000  Gallons  per  minute. 
N.._.  900  Revolutions  per  minute. 
H....     50  Feet. 
P....     90  Brake  horse  power. 

Qx X  Gallons  per  minute. 

Nj.— 1000  Revolutions  per  minute. 

H!_     Y  Feet. 

Px Z  Brake  horse  power. 

By  Formula  (29) 

5000       900  5000  X  1000 

= 0,= =  5555  =  X  Gals,  per  minute 

Qt        1000  900 

By  Formula  (30) 

50=J900)^  50X(100Q)^6L72=Yfeet 

Hx       (1000)2  (900)2 

By  Formula  (31) 

90       (900)3  90  X   (1000)3 

— =_ - Pt  = . —  =124  =  Z  Brake  H- Power 

P1       (1000)3  (900)3 

If  it  is  desired  to  keep  the  revolutions  per  minute  constant, 
and  alter  (Q),  (H)  and  (P),  this  may  be  accomplished  within 
certain  limits  by  changing  the  diameter  of  the  impeller. 

Assume  D  is  the  original  diameter  of  the  impeller  (in  inches 
or  feet)  and  Dx  the  proposed  diameter  of  the  impeller  (in  inches 
or  feet),  and  substituting  these  factors  in  place  of  N  and  N1 
respectively  in  equations  29-31  inclusive,  Qlf  Hj,  and  P1  may 
be  easily  calculated. 


££^ 

122 


n 

ATTLE 

C 

RE 

EK. 

M 

ICH 

IGA 

N,      U. 

S. 

A. 

| 

In  varying  the  conditions  by  changing  the  diameter  of  the 
impeller,  it  should  be  borne  in  mind  that  the  pump  casing  de- 
termines the  maximum  size  of  the  impeller  that  cari  be:  us*ed, 
also,  that  the  diameter  of  the  impeller  cannot  be  "reduced-  be- 
yond a  certain  figure  on  account  of  the  excessive  losses  between 
the  impeller  and  casing. 

Prime  Movers  For  Driving  Centrifugal 

Pumps 

The  majority  of  centrifugal  pumps  in  service  are  motor 
driven.  Care  should  be  exercised  in  choosing  the  size  and  type 
of  motor  to  be  used.  The  exact  capacity  and  rating  of  the  motor 
is  of  great  importance,  especially  where  the  power  is  bought  on 
the  motor  rating.  If  the  motor  is  too  small,  it  is  liable  to  be 
overloaded,  and  if  it  is  too  large  the  customer  pays  for  excess 
power. 

In  choosing  a  motor,  the  maximum  conditions  should  be 
considered,  and  the  power  required  at  rated  speed  and  head 
should  not  in  itself  determine  the  size  of  the  motor. 


Fig.  68. 
Motor-Driven  Centrifugal  Pump. 

Having  determined  the  size  of  the  motor  to  be  used,  the 
next  important  problem  is  to  select  one  of  proper  type  for  the 
service.  If  the  head  must  vary,  this  can  be  accomplished  by 
changing  the  speed  of  the  motor,  and  a  variable  speed  motor 
must  be  selected. 

With  centrifugal  pumps,  squirrel  cage  motors  are  generally 
used  in  the  alternating  current  type,  and  compound  wound 
motors  in  the  direct  motor  type. 

Steam  Engine  and  Miscellaneous 

Since  the  development  of  high  speed  steam  engines,  more 
engine-driven  centrifugal  pumps  have  been  used.  This  type 


123 


A 


of  installation  is  desirable  in  small  plants  where  the  engineer 
is  more  familiar  with  the  engine,  than  the  motor,  or  the  steam 
turbine.  Steam  engine  driven  centrifugal  pumps  are  generally 
low  head  pumps,  and  are  mostly  used  for  circulating  pumps. 


Fig.  69. 

Steam  Engine  Driven  Centrifugal 
Gas  and  Oil  engines  are  extensively  used  direct  connected  to 
centrifugal  pumps.     One  of  the  largest  fields  for  this  type  is  in  con- 
tractor's work  for  emptying  excavations,  sumps,  and  ditches. 


Fig.  70. 
Gas  Engine  Driven  Centrifugal  Pump. 


[  AC  H  I N  E  RY^AIR   C  • 
124 


SOR., 


r 

BATTLE 

C 

REE 

K. 

MICH 

IG 

AN, 

U. 

s. 

A. 

1 

Steam  Turbines 

Centrifugal  pumps  driven  by  steam  turbines  are  used  ex- 
tensively for  boiler  feed,  hot  well  and  circulating  pumps.  These 
installations  are  very  efficient,  compact  and  require  a  minimum 
amount  of  attention  from  the  operator. 


Fig.  71. 
Steam  Turbine  Driven  Centrifugal  Pump. 

In  steam  turbine  driven  units,  the  turbine  may  be  direct 
connected  or  connected  to  the  pump  shaft  by  reducing  gears, 
either  of  which  is  an  economical  drive. 

There  are  four  principal  types  of  steam  turbines. 

First:  The  De  Laval,  an  impulse  turbine  in  which  the 
steam  is  completely  expanded  in  a  single  set  of  nozzles,  and  all 
the  kinetic  energy  is  given  up  in  a  single  row  of  blades. 

Second:  Parsons,  an  impulse-reaction  type  where  the 
energy  of  reaction  of  an  expansion  in  the  moving  blades  is  ad- 
ded to  the  impulse  of  the  steam  as  received  from  the  fixed  noz- 
zles. 

Third:  Zoelly  &  Rateau  impulse  type  having  a  series  of 
partial  expansions,  the  energy  of  each  expansion  being  absorbed 
in  a  single  row  of  moving  blades. 

Fourth:  Curtis,  in  which  the  velocity  of  steam  from  the 
nozzles  is  absorbed  in  and  passes  through  several  rows  of  moving 
blades. 


125 


am««  a  «..,.....  „,«»,,, 


UNION       S  T  E 


PJJ  M  P       COM  P  AN  Y 


Methods  of  Priming  Centrifugal  Pumps 


Fig.  72. 

In  the  cuts  above  are  shown  three  methods  of  priming. 
Fig.  1  shows  a  horizontal  pump  fitted  with  a  discharge  valve 
and  a  steam  ejector.  The  discharge  valve  being  closed,  the 
steam  inlet  valve  to  the  ejector  being  opened  first,  and  then  the 
valve  between  the  ejector  and  the  pump  opened,  the  air  in  the 
pump  and  pipes  will  be  exhausted,  and  the  water  drawn  up  into 
them.  When  the  ejector  is  placed  near  the  pump,  complete 
priming  will  be  indicated  by  water  issuing  from  the  ejector. 
In  shutting  off  the  ejector,  close  the  valve  between  it  and 
the  pump  first,  and  the  steam  inlet  valve  last.  Where  it  is  not 
convenient  to  place  the  ejector  near  the  pump;  the  air  pipe  may 
be  extended,  in  which  case  it  is  necessary  that  a  slightly  larger 
air  pipe  be  used  than  when  the  ejector  is  placed  near  the  pump. 

Fig.  2  shows  a  check  valve  used  in  place  of  the  discharge 
valve  and  a  hand  pump  or  power  vacuum  pump  used  in  place 
of  a  steam  ejector.  The  priming  being  accomplished  by  the 
same  method  as  in  Fig.  1,  there  should  be  a  valve  placed  in  the 
air  pipe  which  must  be  closed  before  starting.  For  hand  prim- 
ing, a  common  pitcher  or  Douglas  pump  may  be  used,  piped  a? 
shown  in  the  cut,  that  is,  with  the  air  pipe  forming  a  loop  a 
little  above  the  discharge.  It  is  only  necessary  to  put  a  little 
water  into  this  style  of  pump  to  water-seal  it,  and  make  of  it 
a  very  good  vacuum  pump,  the  loop  referred  to  above  prevent- 


MA. C  H  I Ng^^AI^^^^^E  SSO  R .S  ^j| 

126 


SiiS^ 


ing  the  water  from  escaping.  When  a  power  driven  vacuum 
pump  is  used  for  priming,  a  water  trap  or  other  means  should 
be  placed  in  the  air  pipe  to  prevent  water  entering  and  pos- 
sibly breaking  the  primer.  Where  the  valves  on  the  vacuum 
pump  are  large,  this  may  be  omitted.  On  large  pumps,  a  water 
glass  similar  to  those  used  on  boilers,  placed  near  the  top  of  the 
pump  shell,  will  show  when  the  priming  is  complete. 

Fig.  3  shows  the  method  of  using  a  foot  valve,  in  which  case 
the  pump  and  suction  pipe  are  to  be  filled  with  water  through 
the  discharge  or  top  of  the  pump  from  any  convenient  source, 
such  as  a  small  tank  or  hand  pump,  which  can  be  piped  to  the 
top  of  the  centrifugal  pump.  Where  the  suction  pipe  is  long, 
there  should  be  at  least  5  feet  of  a  discharge  head  on  the  pump 
to  prevent'the  water  being  thrown  out  of  the  runner  before  the 
water  in  the  suction  line  begins  to  move,  and  thus  cause  failure 
to  start.  It  is  well  to  turn  the  runner  around  once  or  twice  by 
hand  to  insure  getting  all  air  out  of  the  arms,  especially  in  small 
ptimps.  With  vertical  pumps,  where  check  or  discharge  valves 
are  used,  a  vacuum  gauge  placed  on  the  air  priming  pipe  at  the 
head  of  the  well  or  pit  will  show  when  the  pump  is  primed  and 
avoid  climbing  down  into  the  pit  or  well.  A  vacuum  gauge 
may  be  used  in  the  methods  of  priming  shown  in  Figs.  1  and  2, 
but  care  must  be  taken  to  shut  off  the  gauge  before  starting 
the  pump,  as  pressure  will  ruin  a  vacuum  gauge. 

Where  a  pressure  of  water  of  30  or  40  pounds  is  available, 
an  air  ejector  may  be  operated  for  priming,  substituting  water 
for  steam.  This  however,  requires  a  special  ejector. 


AND    CONDENSERS    FOR    EVERY  SERVICE 

127 


UNION       STEAM       PUM  P       COM  PANY 


Suction  Lift — Head  Diagram  for  Centrifugal  Pumps 
Fig.  73. 


I         PUMPING    MACHINERY.   .AIR_C_Q.MPR.ES S_QR_S J 

tf  »ig»'ii"u  .  :  ^•s^trsyrenrLrsnrvwvy  »  lucLULjuj^au^Jt  n  »»»»»»•»»»»•!  » u » mikjc:rn 


128 


|        BATTLE 

C 

REE 

K. 

M 

ICH 

IG 

AN, 

U. 

S. 

A. 

J 

Directions  for  Installing  Centrifugal  Pumps 

Set  base-plate  with  pump  and  prime-mover  on  a  solid  foun- 
dation, preferably  of  concrete,  and  level  carefully;  grout  the  base- 
plate in  and  allow  to  set ;  see  that  pump  and  motor  are  in  line,  and 
shaft  turns  easily  by  hand  after  anehor-bolt  nuts  have  been 
tightened. 

When  pump  is  set,  connect  suction  and  discharge  pipes; 
see  that  these  pipes  are  self-supporting,  in  order  to  avoid  strain 
on  pump  and  insure  proper  alignment. 

Locate  pump  as  near  the  water  supply  as  possible.  The 
maximum  suction  lift  including  pipe  friction,  varies  with  the 
size  of  pump,  and  the  liquids  to  be  handled.  Hot  water  or  heavy 
liquids  must  flow  to  the  pump  under  a  positive  head,  this  head 
varying  according  to  the  difference  in  temperature  of  the  liquid, 
or  the  viscosity  of  the  liquid.  The  diagram  on  page  128  shows 
the  lifts  possible  for  different  sizes  of  pumps  with  varying  tem- 
peratures of  the  water. 

Never  use  pipe  sizes  smaller  than  pump  calls  for.  For  long 
pipe  lines,  use  2  or  3  sizes  larger.  Make  suction  pipe  as  short 
as  possible,  and  avoid  bends  and  elbows.  Make  sure  that  there 
are  no  air  pockets  in  the  line  and  that  the  suction  pipe  is  absolute- 
ly air  tight. 

Place  a  check  valve  and  a  gate  valve  in  the  discharge  pipe, 
as  close  as  possible  to  the  pump.  The  check  valve  must  be  placed 
between  the  gate  valve  and  the  pump  in  order  to  be  able  to  in- 
spect or  repair  the  check  valve  without  being  forced  to  empty 
the  discharge  line. 

Always  provide  a  strainer  on  the  end  of  the  suction  line. 
This  protects  the  pump  from  being  choked  by  foreign  matter, 
and  insures  safe  operation. 

To  avoid  corrosion,  packing  is  removed  from  stuffing  boxes 
before  pump  leaves  factory.  When  repacking,  do  not  draw  the 
glands  up  tight,  but  allow  a  reasonable  leakage,  which  lubricates 
the  packing  and  prevents  the  shaft  being  corroded.  Pipe  the 
leakage  from  the  tap  in  the  bearing  bracket  to  a  sewer  or  drain. 

Before  starting  pump,  clean  the  bearings  with  gasoline  or 
kerosene,  and  fill  oil  reservoirs  with  high  grade  lubricating  oil, 
as  high  as  the  top  of  the  oil  gauge  indicates. 


129 


STEAM       PUMP       COMPANY 


Directions  for  Operating  Centrifugal  Pumps 

The  pump  must  always  be  primed  before  starting,  other- 
wise the  interior  parts  which  depend  upon  the  water  for  lubri- 
cation, will  be  injured.  Never  run  a  centrifugal  pump  empty. 

The  three  methods  of  priming  centrifugal  pumps  are  fully 
described  on  pages  126-127. 

AS  soon  as  case  is  primed  by  either  method,  pump  should 
be  started  with  discharge  valve  closed,  and  brought  up  to  speed. 

Then  open  the  gate  valve  slowly  until  desired  quantity  of 
water  is  obtained.  Failure  of  pressure  to  increase  with  the  speed 
indicates  air  in  the  pump  casing.  In  this  case,  stop  the  pump 
and  prime  again. 

As  long  as  the  water  and  consequently  the  case  do  not  heat 
up  excessively,  due  to  friction  produced  by  the  rotation  of  the 
impeller,  -the  centrifugal  pump  may  be  operated  with  a  closed 
discharge  valve.  In  contrast  with  displacement  pumps,  no 
by-passes  are  required,  nor  can  the  pump  or  the  pipe  system  be 
damaged  as  the  shut-off  pressure  is  only  10  to  15%  greater  than 
the  pressure  at  full  capacity. 

Always  run  the  pump  in  direction  of  arrow  cast  on  case. 
Centrifugal  pumps  can  be  run  only  in  one  direction. 

During  the  operation,  stuffing  boxes  and  bearings  must  be 
inspected  occasionally.  The  centrifugal  pump  does  not  require 
any  other  attention. 

If  the  pump  is  to  be  idle  for  long  periods,  it  should  be  taken 
apart,  cleaned  and  oiled.  This  prevents  parts  rusting  together 
and  preserves  their  good  condition. 

If  pump  is  exposed  to  freezing  temperature,  it  should  be 
drained  immediately  after  stopping. 

These  suggestions  are  intended  to  assist  in  installing  and 
operating  Union  Centrifugal  pumps.  In  all  cases,  successful 
operation  depends  largely  on  correctness  of  installation,  for 
which  this  Company  cannot  be  held  responsible.  For  further 
information  regarding  Union  Centrifugal  Pumps,  write  us. 


130 


MICH 


Some  Centrifugal  Pumps  "Ifs" 

If  after  starting  the  pump  it  throws  a  little  water  at  the 
first  few  revolutions,  and  then  churns  and  fails  to  discharge 
more,  it  is  just  evidence  that  the  air  was  not  all  out  of  the  pump 
and  pipes,  or  the  suction  lift  too  great,  or  a  leaky  pipe,  or  a  long 
suction  and  insufficient  discharge  head. 

If  when  first  started  the  pump  throws  a  full  stream  for  a 
few  minutes,  and  then  fails,  it  is  caused  by  failure  of  supply, 
or  water  receding  in  the  well  below  the  suction  limit,  which  in 
a  well  is  best  determined  by  a  vacuum  gauge  placed  on  the  suc- 
tion elbow  of  the  pump.  The  remedy  for  this  is  to  lower  the 
pump,  thus  reducing  the  suction  lift. 

If  the  pump  delivers  a  full  stream  of  water  at  the  surface, 
or  level  of  the  pump,  but  fails  to  pump  at  a  higher  discharge 
point,  the  speed  of  the  pump  is  too  low. 

If  the  pump  starts  a  full  stream,  and  then  the  discharge 
decreases  very  slowly  until  the  pump  fails  to  deliver  any  water, 
it  is  caused  by  an  air  leak  at  the  packing  gland. 

If  the  pump  delivers  a  full- quantity  for  a  few  hours  and  fails, 
the  speed  and  water  supply  being  unchanged,  the  suction  pipe 
or  impeller  is  obstructed. 

If  when  running  there  is  a  heavy  vibration,  the  shaft  has 
been  sprung,  the  pump  is  out  of  alignment,  or  an  obstruction 
has  lodged  in  one  side  of  the  impeller. 

If  the  bearings  heat  unduly,  the  belt  is  unnecessarily  tight, 
the  bearings  lack  oil,  or  there  is  an  end  thrust. 

The  last  "If"  is,  that  if  the  pump  is  properly  installed, 
and  operating,  it  will  positively  operate  successfully,  as  the 
centrifugal  is  the  most  simple,  most  efficient  and  long  lived 
water  lifting  device  manufactured. 

In  pumping  hot  water  or  fluids,  the  suction  lift  of  the  pump 
must  be  as  small  as  possible  on  account  of  the  lowering  of  the 
boiling  point  under  vacuum,  and  consequent  loss  of  priming 
from  the  presence  of  vapor. 

Water  should  not  discharge  into  a  sump  or  tank  near  the 
end  of  the  suction  pipe,  as  there  is  danger  of  carrying  air  down, 
and  into  the  suction  pipe. 

Do  not  attempt  to  pump  more  than  the  maximum  catalogue 
rating  of  the  pump,  as  that  will  cause  waste  of  power. 

Do  not  call  for  help  until  you  are  sure  none  of  the  above 
"Ifs"  are  present. 


To  Calculate  Horse  Power 

To  determine  the  theoretical  horse  power  to  elevate  a  given 
quantity  of  water  to  a  given  height,  multiply  the  number  of 
gallons  delivered  per  minute  by  8.33  (weight  of  one  gallon  of 
water),  multiply  this  result  by  the  total  head,  and  divide  this 
result  by  33000  (33000  pounds  elevated  one  foot  in  one  minute 
equals  one  horse  power).  This  formula  is  the  theoretical  horse 
power,  and  when  simplified  is : 

H.  P.  =.000252  x  Gallons  per  minute  X  'Head  in  feet.     (32) 

To  determine  the  actual,  or  brake  horse  power,  divide  the 
theoretical,  or  water  horse  power  by  the  efficiency  of  the  pump. 

EXAMPLE:  It  is  desired  to  elevate  200  gallons  of  water 
per  minute,  to  an  elevation  of  150  feet  through  200  lineal  feet 
of  3*  pipe  with  three  3  "-90°  elbows,  and  one  3"  globe  valve. 

The  friction  loss  of  200  gallons  per  minute  through  200'  of 
3"  pipe  from  the  table,  on  page  145  =  11. 54X2  =23.08'. 

The  friction  loss  of  200  gallons  per  minute  through  three 
3"-90°  elbows  from  the  table,  on  page  147-1.18  X  3  =  3.54'. 

The  friction  loss  of  200  gallons  per  minute  through  one  3" 
globe  valve  from  the  table  on  page  148,  is  equivalent  to  24 
lineal  feet  of  3"  straight  pipe,  and  from  the  table  on  page  145, 
the  friction  loss  of  200  gallons  per  minute  through  24'  of  3  "  pipe 
=  11.54  X  -£•  =  2.76'. 

The  total  head,  therefore  is  equal  to  the  sum  of  the  above 
heads  or 

Friction  head  in  pipe  =  23.08' 
Friction  head  in  elbows  =  3.54' 
Friction  head  in  valve  =  2.76' 
Static  Head  =150.00' 

Total  head  -179.38' 

The  theoretical  or  water  horse  power,  equals  from  formula 
(32) 

.000252X200X179.38=9.1  =Water   horse   power. 

Assuming  an  efficiency  for  the  pump  of  55%, the  actual 
or  brake  horse  power  necessary  to  operate  the  pump  = 

9.1  X  100 

— =  16.5  Brake  horse  power. 

oo 

So,  in  choosing  a  motor  for  these  conditions,  it  would  be 
advisable  to  use  a  20  horse  power  motor,  as  the  nearest  %sizc, 
which  is  15  horse  power,  is  too  small,  and  would  be  overloaded. 
The  20  horse  power  motor  allows  a  margin  for  unforeseen  future 
changes  in  operating  conditions,  which  might  increase  the  load. 


132 


It 

B  AT 

TLE 

C  REEK, 

M 

ICH 

IG 

AN, 

U. 

S. 

A. 

J 

Cost  of  Pumping 

The  total  cost  of  pumping  is  the  sum  of  the  operating 
expenses,  and  the  fixed  charges.  The  former  consists  of  labor, 
fuel,  electric  current,  supplies,  etc.  The  latter  consists  of  in- 
terest on  the  first  cost,  insurance,  taxes,  depreciation  and  ad- 
ministration. 

The  first  cost  covers  the  cost  of  pumping  equipment.  The 
total  annual  cost  consists  of  fixed  charges  and  operating  costs 
for  a  year.  The  cost  of  pumping  per  water  horse  power,  per 
1000  gallons  per  minute,  or  any  similar  unit,  is  the  total  annual 
cost  divided  by  the  total  capacity  of  the  pump  in  these  units. 

It  is  a  minimum  when  the  pump  is  not  operated,  as  it  will 
consist  only  of  fixed  charges,  and  is  a  maximum  when  the  pump 
is  running  continuously,  as  it  will  make  the  operating  expenses 
a  maximum. 

On  a  steam  driven  pumping  unit,  such  as  a  steam  turbine, 
or  engine  driven  pump,  or  a  fly  wheel  pumping  engine 

T        Q  X  8.33  X  II  X  C 

-^-  -  -f  L  -f-  F(i-hd  +  t)  fa    (33) 

in  which 

T    -Total  Annual  Cost 

Q    =  Total  number  of  gallons  pumped  per  year. 

H   =  Head  in  feet. 

C    =  Cost  of  steam  per  1000  Ibs. 

D   =Duty  in  foot  pounds  for  1000  Ibs.  of  steam. 

L    =  Labor  cost,  etc. 

F    =  Total  investment 

i     =  Interest  rate  on  the  investment. 

d    =Rate  of  depreciation. 

t     =  Taxes  and  insurance. 

a    =  Administration  costs. 

In  an  electric  driven  pumping  unit,  it  is  necessary  to  con- 
sider the  cost  per  1,000,000  B.  T.  U.  supplied  the  motor  instead 
of  C.,  in  the  above  equation.  (1  K.  W.  Hr.  =3412  B.  T.  U.) 
Then  D.  =  Duty  in  foot  pounds  per  1,000,000  B.  T.  U.  supplied 
to  the  motor. 

Since  1  B.  T.  U.=778  foot  pounds,  1,000,000  B.  T.  U.  = 
778,000,000  foot  pounds,  and  Duty  =778,000,000  X  efficiency 
of  the  unit.  Therefore,  the  above  equation  transformed  on 
this  basis,  assuming  K  =  the  cost  of  the  electricity  per  K.  W.  Hr.,  is 


|j«»iiniiiiiaa»flBaBn;B^AAAJL»J!«^*«»«inrariira 

jjL^AND    CONDENSERS 

frAJL»JgA^» 

FOR 

EVERY 

SERVICE 

1 

133 


TTNTl  OK       STEAM       PUMP 


T  ~ 


QX8.33XHXK 


+F(i  +d  +t)  +a 


2,655,000  Xefficiency  of  unit. 
From  the    above  equation,  it  is  apparent  that  if  the  cost 
of  power  is  high,   it  is  an  economical  investment  to  buy  an 
efficient  pump. 

Pumping  Liquids  Other  Than  Water  With 
Centrifugal  Pumps 


GffVGE  SHOWS 
/OOrr.  OK  43  POUNDS. 


GAUGE  SHOWS 
/OOx/3.6-/36Orr 

OR  S9O  PQVNBS 


WATER  MERCURY 

In  order  to  make  a  drastic  comparison,  assume  two  identical 
pumps,  discharging  under  the  same  conditions  and  both  running 
at  the  same  speed.  Pump  No.  1  will  handle  water  and  pump 
No.  2  will  handle  mercury.  The  static  head  in  both  cases  will 
be  100  feet.  The  pumps  are  started,  and  it  is  observed  that  both 
the  water  column  and  the  mercury  column  will  stand  exactly 
at  the  same  height  in  the  standpipe.  This  is  explained  by  the 
fact  that  the  head  created  by  a  centrifugal  pump  is  not  a  pressure 
head,  but  a  velocity  head.  This  velocity  head  depends  entirely 
on  the  velocity  of  the  water,  which  velocity  in  turn  was  produced 
by  the  speed  of  the  impeller.  As  both  pumps  run  at  the  same 
speed,  both  liquids  regardless  of  their  specific  gravity  or  weight 
will  stand  at  the  same  height  in  the  standpipe. 

The  difference  in  the  weight  of  the  liquids  is  shown  by  the 
pressure  gauges.  Let  us  assume  that  the  pipe  line  is  very  large, 
so  that  pipe  friction  can  be  neglected.  Both  gauges  will  show 
the  pressure  of  the  column  of  liquid  in  the  respective  pipes. 
The  gauge  No.  1  will  read  100  ft,  or  43  Ibs.,  which  is  the  weight 


134 


per  square  inch  of  water  column  100  ft.  high.  As  mercury  is  13.6 
times  heavier  than  water,  gauge  No.  2  will  show  13.6  X  100 
1360  ft.  or  590  Ibs.  pressure. 

The  power  required  by  these  two  identical  pumps,  handling 
different  liquids,  can  easily  be  computed,  considering  that  re- 
gardless of  the  method,  whether  the  head  is  obtained  by  centri- 
fugal force  or  by  piston  pressure,  the  power  required  for  pump- 
ing any  kind  of  liquid  is  always  the  product  of  the  weight  of 
the  liquid  and  the  height  it  has  to  be  elevated.  Therefore, 
should  the  pump  No.  1,  which  handles  water,  require  10  H.  P., 
the  pump  No.  2  will  require  13.6  X  10  =  136  H.  P.,  as  both 
pumps  work  against  the  same  head,  with  the  only  difference 
that  No.  2  handles  a  liquid  13.6  times  heavier  than  No.  1. 

Nothing  has  been  said  about  the  volume  of  the  liquid 
handled.  As  both  pumps  have  the  same  dimensions,  it  is  self- 
evident  that  they  will  deliver  the  same  volume  of  different 
liquids,  as  long  as  the  viscosity  does  not  enter  into  the  question. 

Recapitulation :    In  summing  up  we  find : 

(1)  Regardless  of  the  specific  gravity  of  the  liquid,  a  cen- 
trifugal pump  will  always  produce  the  same  static  head. 

(2)  The  pressure  (read  on  the  pressure  gauge  at  the  discharge 
of  the  pump)   will  be  increased  in  proportion   to  the  specific 
gravity. 

(3)  The  horse-power  required  by  the  pump  will  also  be 
increased  in  proportion  to  the  specific  gravity. 

EXAMPLES:  (1)  Suppose  a  pump  is  required  to  elevate 
brine  of  1.2  specific  gravity  to  a  static  head  of  100  ft.  As  ex- 
plained before,  any  pump  suitable  for  lifting  water  to  a  static 
head  of  100  ft.,  will  also  lift  brine  to  the  same  height.  The 
pressure  gauge  will  register  the  weight  of  a  column  of  brine  100 
ft.  high.  A  column  of  water  100  ft.  high  would  show  43  Ibs. 
pressure.  As  brine  is  1.2  times  heavier  than  water,  the  gauge 
will  show  43  X  1.2  =52  Ibs.  pressure. 

Assuming  that  it  required  10  H.  P.  to  drive  the  water  pump, 
the  brine  pump  will  require  1.2  X  10  =  12  H.  P. 

(2)  Suppose  a  pump  is  required  to  pump  the  same  brine 
of  1.2  specific  gravity  against  a  pressure  of  43  Ibs.  This  time 
43  Ibs.  are  required  on  the  pressure  gauge  of  the  brine  pump. 
But  if  a  water  pump  of  proper  proportions  to  discharge  against 
100  ft.  or  43  Ibs.  is  used,  the  gauge  would  show  52  Ibs.  when 
handling  brine,  as  explained  before.  Therefore,  to  reduce  this 
pressure  to  the  required  43  Ibs.,  it  is  necessary  to  change  the 
impeller  accordingly. 


135 


As  seen  in  example  No.  1,  it  required  10  H.  P.  to  work 
against  43  Ibs.  water  pressure.  Naturally  it  takes  the  same 
10  H.  P.  to  pump  against  43  Ibs.  brine  pressure. 

In  most  cases  the  brine  pumps  are  used  as  circulating 
pumps  and  work  against  a  balanced  head;  in  other  words,  the 
pump  has  only  to  overcome  the  pipe  friction.  Therefore  the 
head  for  such  a  case  has  to  be  specified  as  a  pressure  head,  and 
not  as  a  static  head.  This  is  insignificant  .for  small  installations; 
for  larger  installations,  however,  it  will  mean  using  a  smaller 
motor  (for  instance  50  H.  P.  instead  of  75  H.  P). 

(3)  Suppose  a  pump  is  required  to  deliver  gasoline  of  0.8 
specific  gravity  against  a  static  head  of  100  ft. 

Figured  for  water,  the  pump  will  require  say  10  H.  P. 
As  the  pump  will  have  to  work  against  a  static  head  of  100  ft., 
the  pressure  gauge  will  read  only  80  ft.  (corresponding  to  a 
specific  gravity  of  0.8),  and  the  pump  will  require  10  X  0.8  =  8 
H.  P.  only. 

(4)  Suppose  a  pump  is  required  to  handle  gasoline  of  0.8 
specific  gravity  against  a  pressure  of  43  Ibs. 

This  time  43  Ibs.  are  required  on  the  pressure  gauge  of  the 
pump;  therefore,  if  the  gasoline  pump  is  designed  like  the  water 
pump,  only  34  Ibs.  would  be  shown  by  the  pressure  gauge,  cor- 
responding to  the  weight  of  the  gasoline  column.  Therefore, 
in  order  to  obtain  43  Ibs.  pressure  with  gasoline,  it  is  necessary 
to  increase  the  impeller  sufficiently  to  give  43  Ibs.  pressure  on 
the  gauge.  This  pump,  of  course,  will  require  10  H.  P.,  exactly 
the  same  amount  as  required  for  water  pumping  against  43  Ibs. 

As  to  liquids  of  thick  consistency,  regardless  of  their  specific 
gravity,  it  is  general  experience  that,  compared  with  water, 
a  pump  delivers  less  capacity  and  requires  more  horse -power 
to  drive  it.  This  is  explained  by  the  fact  that  the  thick  liquid 
produces  more  skin  friction  and  therefore  offers  more  internal 
resistance  to  the  moving  parts  of  the  pump.  No  general  rule 
has  been  established  yet,  and  in  cases  of  doubt,  experiment  is 
the  only  way  to  find  out  the  conditions.  Therefore,  should  any 
cases  arise  where  thick  liquids  are  to  be  handled,  it  is  necessary 
to  provide  ample  power.  In  chemical  plants,  sugar  mills,  etc., 
it  is  general  practice  to  heat  heavy  liquids  so  they  will  flow 
freely  and  then  pump  them  with  centrifugal  pumps.  In  such 
cases  the  liquid  should  always  flow  to  the  pump  under  a  suction 
head.  This  is  also  necessary  for  hot  water,  acids  and  for  any 
liquids  where  vaporization  is  liable  to  occur. 

136 


B ATt  L  E       C  RE  E  K . 


ICHIGAN,     U.  S 


Material  Used 

—  All  bronze  fitted 
All  bronze  fitted 
All  bronze  fitted 
-  -  All  iron  fitted 

3TM 

§1.! 

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I! 

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I 

Chemical  Symbol 

C2H402 
C2H4O2  +  H2O 

Neutral 
CNOH+H2O 
MnOH  +  H2O 
KOH+H2O 

NH3+H2O 

£ 
8 

1 

3 
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Acetic  Aid,  Concentrated  

Acetic  Acid,  Diluted  ...  . 
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'S 

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QJ 

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1  — 

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Caustic  Chloride  of  Magnesium 
Solution,  Cold  
Caustic  Cyanogen  in  Solution  
Caustic  Manganese  in  Solution  
Caustic  Potash  Solution  

CD  __ 
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I 

cr 

l| 
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AND    CONDENSERS    FOR    EVERV  SERVICE 


137 


The  Materials  Used  for  Pumping  Various  Liquids  Continued 

Material  Used 

1 

<G 

c 

< 

"3 

< 

11 

<< 

< 

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1 

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t 

y: 

s 

£ 

PC 

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<<<<<     £<<<« 

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Chemical  Symbol 

NaOH+H2O 
NaClOH+H20 
ZnClOH+HO 
Cl 
KC1+H2O 

C6H4CH3OH 
C2N2 

KCN+H2O 

1 

C3H8O3 

FeSo4+7H2O 

U 

3 
.2* 

3 

tx 

i 

^^^. 

0. 

1 

"1 

j 

ic  Potash  Niter  in  Solution  
LC  Soda  Solution  
c  Sodium  Chloride  Solution  .... 
LC  Zinc  Chloride  
ne 

de  of  Potash  Solution  
LC  Chloride  of  Magnesium 
iltition.  Hot 

',«_ 
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Distillery  wort  
Ferrous  Chloride. 
Oasolinp 

1 
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Guncotton  Brine. 
Hpaw  Oil 

11  lijj  8  ' 

oJ   rt    OS   cti  A  A  ctf 

oououuo 

138 


^ 


The  Materials  Used  for  Pumping  Various  Liquids  Continued 

Material  Used 

c 

C 
1 

^- 
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c  e 

IJ 
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(Continued  on  next  page.} 

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Chemical  Symbol 

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Sugar  Comoound.... 

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I 
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Milk  
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AND    CONDENSERS    FOR    EVERY  SERVICE 

--- 


|        UNION 

S  TEAM 

PUMP 

COM  P  ANY 

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I    c 


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oj    •*-<   F5 
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PQ    4J  ^ 


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8    S  g 

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AIR    CQMPRJESS^ORg, 


140 


]T     BATTLE 

C 

RE 

EK, 

M 

ICH 

IG 

AN. 

u. 

s. 

A. 

3 

Consumption  of  Gasoline  For  Pumping 


Approximate    Consumption  of  Gasoline  or  Distillate  per 
24  Hours  when  Pumping  100  Gallons  per  Minute 

Consumption  of  Gasoline  or 

100  Feet  Head. 

Distillate  per  Effective 

In  Gallons. 

In  Gallons. 

Total  Efficiency  of  Pump  and  Drive. 

30  percent. 

40  percent. 

50  per  cent. 

60  per  cent. 

70  per  cent. 

Ho 

20 

15. 

12. 

10. 

8.7 

H 

22.5 

17. 

13.6 

11.3 

9.6 

H 

25.5 

19.2 

15.2 

12.8 

10.9 

% 

29. 

21.5 

17.2 

14.4 

12.3 

Ve 

33.5 

25. 

20. 

16.7 

14.3 

% 

40. 

30. 

24. 

20. 

17.3 

To  find  the  approximate  number  of  gallons  of  gasoline  or 
distillate  required  per  hour  when  pumping  600  to  1,200  gallons 
per  minute,  multiply  the  water  horse  power  by  .027,  or  when 
pumping  100  to  500  gallons  per  minute,  multiply  by  .032. 

The  water  horse  power  is  found  by  multiplying  the  weight 
of  water  pumped  per  minute  by  the  total  height  in  feet,  and 
dividing  by  33,000. 

Another  method  of  calculating  the  theoretical  water  horse 
power  is  to  multiply  the  gallons  per  minute  by  the  total  head 
in  feet,  including  friction  in  the  pipes,  and  dividing  by  4,000. 


Consumption  of  Electric  Current  For  Pumping. 


Total    Efficiency 

Consumption  of  Electric 
Current  in  Kilowatt  Hours 

Total  Efficiency 

Consumption  of  Electric 
Current  in  Kilowatt  Hours 

of   Pump,    Motor 
and  Transformer. 

per  24  Hours  Run,  Pumping 
100  Gallons  per   Minute  100 

of  Pump,    Motor 
and  Transformer. 

per  24  Hours  Run,  pumping 
100  Gallons  per  Minute  100 

Feet  High. 

Feet  High. 

Per  Cent. 

Kilowatt  Hours. 

Per  Cent. 

Kilowatt  Hours. 

30 

149.2 

45 

100. 

32 

142. 

50 

89. 

34 

132. 

55 

81. 

36 

124. 

60 

75. 

38 

118. 

65 

69. 

40 

112. 

ro 

64. 

42 

107. 

75 

59. 

The  approximate  kilowatt  hours  are  equal   to    the    horse 
power  consumed  by  the  pump  divided  by  1.1. 


141 


1 


UNION       STEAM       PUMP       COMPANY 


Heads  in  Feet  of  Water  with  Equivalent  Inches 

of  Mercury,  Pounds  per  Sq.  In.  and 

Velocity  in  Ft.  per  Sec. 

Computed  with  following  Constants:  g==  acceleration  of  gravity=32.16; 
sv=weight  of  cubic  foot  of  water=62.4;  Specific  gravity  of  mercury 
=13.6. 


1 

il 

Inches  of 
Mercury 

Pounds 
per  Sq.  In. 

Velocity 
Ft.  per  Sec. 

Head  in 
Feet 

Inches  of 
Mercury 

Pounds 
per  Sq.  In. 

Velocity 
Ft.  per  Sec. 

1 
2 

.883 
1.765 

.433 

.866 

8.02 
11.34 

50 
51 

44.2 
45. 

21.66 
22.09 

56.6 
57.3 

3 

2.65 

1.30 

13.89 

52 

45.9 

22.54 

57.8 

4 

3.53 

1.73 

16.04 

53 

46.8 

22.98 

58.4 

5 

4.41 

2.17 

17.93 

54 

47.7 

23.40 

59.0 

6 

5.30 

2.60 

19.65 

55 

48.5 

23.84 

59.5 

7 

6.18 

3.03 

21.22 

56 

49.4 

24.27 

60.0 

8 

7.06 

3.47 

22.69 

57 

50.3 

24.71 

60.6 

9 

7.95 

3.90 

24.06 

58 

51.2 

25.13 

61.2 

10 

8.83 

4.33 

25.36 

59 

52.1 

25.58 

61.6 

11 

9.71 

4.76 

26.60 

60 

53. 

26.00 

62.1 

12 

10.6 

5.19 

27.78 

61 

53.8 

26.43 

62.6 

13 

11.5 

5.63 

28.92 

62 

54.7 

26.87 

63.2 

14 

12.35 

6.06 

30.01 

63 

55.6 

27.31 

63.7 

15 

13.25 

6.49 

31.06 

64 

56.5 

27.74 

64.2 

16 

14.10 

6.92 

32.08 

65 

57.3 

28.19 

64.7 

17 

15.00 

7.36 

33.07 

66 

58.2 

28.60 

65.2 

18 

15.9 

7.79 

34.03 

67 

59.2 

29.03 

65.6 

19 

16.78 

8.23 

34.96 

68 

60. 

29.47 

66.2 

20 

17.65 

8.66 

35.87 

69 

60.9 

29.91 

66.6 

21 

18.52 

9.09 

36.75 

70 

61.8 

30.34 

67.1 

22 

19.41 

9.12 

37.62 

71 

62.7 

30.79 

67.6 

23 

20.3 

9.96 

38.46 

72 

63.5 

31.20 

68.1 

24 

21.2 

10.40 

39.29 

73 

64.5 

31.63 

68.5 

25 

22.1 

10.83 

40.10 

74 

65.3 

32.07 

69.0 

26 

22.95 

11.27 

40.90 

75 

66.2 

32.51 

69.5 

27 

23.8 

11.67 

41.67 

76 

67.1 

32.95 

70.0 

28 

24.7 

12.12 

42.44 

77 

68. 

33.39 

70.5 

29 

25.6 

12.56 

43.19 

78 

68.9 

33.81 

71.0 

30 

26.5 

13.00 

43.93 

79 

69.75 

34.24 

71.4 

31 

27.4 

13.42 

44.66 

80 

70.6 

34.67 

71.8 

32 

28.25 

13.87 

45.37 

81 

71.5 

35.10 

72.2 

33 

29.1 

14.30 

46.07 

82 

72.4 

35.53 

72.7 

34 

30. 

14.72 

46.77 

83 

73.3 

35.98 

73.1 

35 

30.9 

15.16 

47.45 

84 

74.1 

36.40 

73.5 

36 

31.8 

15.60 

48.12 

85 

75. 

36.83 

74.0 

37 

32.65 

16.02 

48.79 

86 

75.9 

37.28 

74.5 

38 

33.6 

16.47 

49.44 

87 

76.8 

37.71 

74.8 

39 

34.4 

16.90 

50.09 

88 

77.7 

38.14 

75.3 

40 

35.3 

17.33 

50.72 

89 

78.6 

38.78 

75.7 

41 

36.2 

17.77 

51.35 

90 

79.5 

39.00 

76.2 

42 

37.1 

18.20 

51.98 

91 

80.3 

39.42 

76.6 

43 

37.95 

18.62 

52.59 

92 

81.2 

39.84 

77.0 

44 

38.8 

19.07 

53.20 

9;] 

82. 

40.3 

77.5 

45 

39.7 

19.50 

53.80 

94 

83. 

40.7 

77.8 

46 

40.6 

19.93 

54.40 

95 

83.8 

41.2 

78.1 

47 

41.5 

20.36 

54.98 

96 

84.7 

41.6 

78.6 

48 

42.4 

20.80 

55.57 

97 

85.6 

42.1 

79.0 

49 

43.3 

21.24 

56.14 

98 

86.5 

42.5 

79  5 

142 


BAT  T  L  E      CREEK.     M  IQHJ  CLAN  ,_U._  S_._A 


Heads  in  Feet  of  Water  with  Equivalent   Inches 

of  Mercury,  Pounds  per  Sq.  In.  and 

Velocity  in  Ft.  per  Sec. 

(Continued) 

Computed  with  following  Constants:  g=acceleration  of  gravity =3 2. 16; 
w=weight  of  cubic  foot  of  water=62.4;  Specific  gravity  of  mercury 
=13.6. 


c 
•0^, 

II 

Inches  of 
Mercury 

Pounds 

per  Sq.  In. 

Velocity 
Ft.  perSec. 

Head 
in  Feet 

Inches  of 
Mercury 

Pounds 
per  Sq.  In. 

Velocity 
Ft.  per  Sec. 

99 

87.4 

42.9 

79.8 

400 

353. 

173.3 

160.1 

100 

88.3 

43.3 

80.2 

410 

362. 

177.7 

162.2 

105 

92.7 

45.4 

82.25 

420 

371. 

182.0 

164.4 

110 

97.1 

47.6 

84.2 

430 

379.5 

186.2 

166.0 

115 

101.5 

49.8 

86.0 

440 

388. 

190.7 

168.1 

120 

105.9 

51.9 

88.0 

450 

397. 

195.0 

170.0 

125 

110.3 

54.1 

89.8 

460 

406. 

199.3 

172.0 

130 

114.8 

56.3 

91.5 

470 

450. 

203.6 

174.0 

135 

119. 

58.4 

93.2    ' 

480 

424. 

208.0 

176.0 

140 

123.5 

60.6 

95.0 

490 

432. 

212.4 

177.7 

145 

128. 

62.7 

96.5 

500 

441. 

216.6 

179.5 

150 

132.3 

64.9 

98.2 

510 

450. 

220.9 

181.0 

155 

136.8 

67.1 

100.0 

520 

458. 

225.4 

183.0 

160 

141.1 

69.3 

101.3 

530 

468. 

229  .  8 

184.4 

165 

145.7 

71.4 

103.0 

540 

477. 

234.0 

186.1 

170 

150. 

73.6 

104.7 

550 

485. 

238.4 

188.0 

175 

154.4 

75.8 

106.1 

560 

494. 

242.7 

190.0 

180 

159. 

77.9 

107.5 

570 

503. 

247.1 

191.6 

185 

163.2 

80.1 

109.0 

580 

512. 

251.3 

193.0 

190 

167.7 

82.2 

110.5 

590 

521. 

255.8 

194.9 

195 

172. 

84.4 

112.0 

600 

529. 

260.0 

196.2 

200 

176.5 

86.6 

113.3 

620 

548. 

268.7 

199.9 

210 

185.2 

90.9 

116.2 

640 

565. 

277.4 

201.4 

220 

194. 

95.2 

119.0 

660 

583. 

286.0 

206.0 

230 

203. 

99.6 

121.8 

680 

600. 

294.7 

209.0 

240 

212. 

104.0 

124.2 

700 

618. 

303.4 

212.0 

250 

226. 

108.3 

127.0 

720 

635. 

312.0 

215.0 

260 

229.5 

112.7 

129.2 

740 

653. 

320.7 

218.0 

270 

238.1 

116.9 

132.0 

760 

671. 

329.5 

221.0 

280 

247. 

121.2 

134.2 

780 

688. 

338.1 

224.0 

290 

256. 

125.6 

136.6 

800 

706. 

346.7 

226.5 

300 

265. 

130.0 

139.0 

820 

724. 

355.3 

230.0 

310 

274. 

134.2 

141.0 

840 

742. 

364.0 

232.0 

320 

282. 

138.7 

143.3 

860 

758. 

372.8 

235.0 

330 

291. 

143.0 

146.0 

880 

.776. 

381.4 

238.0 

340 

300. 

147.2 

148.0 

900 

794. 

390.0 

240.5 

350 

309. 

151.6 

150.0 

920 

812. 

398.4 

243.3 

360 

318. 

156.0 

1  52  .  0 

940 

830. 

407.0 

246.0 

370 

326.5 

160.2 

154.0 

960 

847. 

416.0 

248.5 

380 

335. 

164.7 

156.1 

980 

865. 

425.0 

251.0 

390 

344. 

169.0 

158.2 

1000 

883. 

433.0 

253.8 

143 


Table  of  Friction  of  Water  in  Pipes 


Giving  the  velocity  in  feet  per  sec.,  the  friction  head  in  feet,  and  friction  loss  in  Ibs.  pressure  per  sq.  in. 

for  each  100  feet  in  length   of   pipe,  for  different  sizes  of  clean  iron  pipe 

discharging  given  quantities  per  minute. 


Gallons  per 

minute 

Velocity 
in  feet 
per  second  || 

is! 

aas 

41 

•S.Scr 

.y  w  £ 

C  OT  5 

fo^o. 

Velocity 
in  feet 
per  second  || 

thl 

gs.s 

Friction 
loss  in  Ibs. 
per  sq.  in. 

£•    ° 

II  i 

231 

1*31 

£w.s 

iW 

0    rp 

'C  n  & 
Pn.2  0. 

Velocity 
in  feet 
per  second 

g 

-S-d  « 

0   rt£ 

'C  « 

£E.S 

Friction 
loss  in  Ibs. 
per  sq.  in.  |{ 

%" 

1" 

IV 

IV 

5 

3.64 

7.59 

3.3 

2.04 

1.93 

0.84 

1.3 

0.71 

0.31 

0.91 

0.27 

0.12 

10 

7.28 

29.90 

13.0 

4.08 

10.26 

3.16 

2.6 

2.41 

1.05 

1.82 

1.08 

0.47 

15 

10.92 

66.01 

28.7 

6.12 

16.05 

6.98 

3.9 

5.47 

2.38 

2.73 

2.23 

0.97 

20 

14.56 

115.92 

50.4 

8.16 

28.29 

12.30 

5.2 

9.36 

4.07 

3.64 

3.81 

1.66 

25 

18.2 

180.00 

78.0 

10.20 

43.70 

19.0 

6.5 

14.72 

6.4 

4.55 

5.02 

2.62 

30 

12.24 

63.25 

27.5 

7.8 

21.04 

9.15 

5.46 

8.62 

3.75 

35 

—  —  — 

4" 

~—  — 

12.28 

85.10 

37.0 

9.1 

28.52 

12.4 

6.37 

11.61 

5.05 

40 

1.04 

0.  1383 

0.06 

10.32 

110.40 

48.0 

10.4 

37.03 

16.1 

7.28 

14.99 

6.52 

45 

.17 

0.1615 

0.07 

11.7 

46.46 

20.2 

8.19 

18.74 

8.15 

50 

.3 

0.208 

0.09 

" 

5" 

13. 

57.27 

24.9 

9.1 

23.00 

10.0 

60 

.56 

0.3 

0.13 

0.88 

0.1156 

0.05 

15.6 

85.50 

87.0 

10.92 

32.95 

14.25 

70 

.82 

0.439 

0.19 

1.04 

0.162 

0.07 

18.2 

114.00 

49.3 

12.74 

44.6 

19.3 

75 

.95 

0.485 

0.21 

1.2 

0.174 

0.075 

19.5 

129.00 

56.1 

13.65 

51.52 

22.4 

80 

2.08 

0.581 

0.23 

1.28 

0.185 

0.08 

14.56 

58.45 

25.3 

90 

2.34 

0.6 

0.26 

1.44 

0.208 

0.09 

6" 

16.38 

81.5 

35.25 

100 

2.60 

0.763 

0.33 

1.6 

0.277 

0.12 

1.14 

0.115 

0.05 

89.70 

39.0 

125 

3.25 

1.13 

0.49 

2. 

0.393 

0.17 

1.42 

0.161 

0.07 

•"""•• 

7" 

- 

150 

3.8 

1.59 

0.69 

2.4 

0.578 

0.25 

1.71 

0.231 

0.10 

1.2 

0.0924 

0.04 

175 

4.45 

2.146 

0.93 

2  S 

0.785 

0.34 

2. 

0.302 

0.13 

1.38 

0.115 

0.05 

185 

4.7 

2.484 

1.075 

2.96 

0.84 

0.363 

2.11 

0.36 

0.155P 

1.55 

0.13 

0.0562 

200 

5.1 

2.82 

1.22 

3.2 

0.972 

0.42 

2.28 

0.393 

0.17 

1.7 

0.162 

0.07 

250 

6.4 

4.37 

1.89 

4. 

1.504 

0.65 

2.8 

0.601 

0.26 

2.1 

0.2775 

0.12 

265 

6.79 

4.645 

2.09 

4.24 

1.69 

0.731 

3.03 

0.70 

0.303 

2.23 

0.31 

0.134 

300 

7.6 

6.15 

2.66 

4.8 

2.15 

0.93 

3.4 

0.85 

0.37 

2.4 

0.393 

0.17 

350 

8.9 

8.44 

3.65 

5.6 

2.914 

1.26 

3.9 

1.15 

0.50 

2.94 

0.531 

0.23 

370 

9.41 

9.33 

4.04 

5.92 

3.197 

1.382 

4.22 

1.33 

0.576 

3.1 

0.59 

0.255 

400 

0.1 

10,92 

4.73 

6.5 

3.72 

1.61 

4.5 

1.50 

0.65 

3.36 

0.693 

0.30 

450 

1.4 

13.88 

6.01 

7.3 

4.62 

2.00 

5.05 

1.87 

0.81 

3.96 

0.855 

0.37 

480 

2.16 

14.34 

6.21 

7.68 

5.06 

2.192 

5.49 

2.16 

0.935 

4.03 

0.96 

0.415 

500 

2.7 

17.16 

7.43 

8.1 

5.55 

2.40 

5.6 

2.22 

0.96 

4.2 

1.04 

0.45 

750 

14" 

12.15 

11.28 

4.875 

8.4 

5.11 

2.21 

6.3 

2.34 

1.03 

1000 

2.224 

0.1432 

0.062 

11.3 

8.98 

3.88 

8.4 

4.16 

1.80 

1100 

2.444 

0.18 

0.078 

12.57 

10.90 

4.715 

9.25 

5.08 

2.20 

1250 

2.78 

0.22 

0.0952 

15" 

14.1 

13.86 

6.00 

10.5 

6.60 

2.85 

1500 

3.336 

0.306 

0.135 

2.7 

0.22 

0.0952 

18" 

12.6 

9.45 

4.08 

2000 

4.448 

0.541 

0.234 

3.6 

0.38 

0.  1645 

2.74 

0.195 

0.0844 

2200 

4.9 

0.68 

0.2943 

3.96 

0.455 

0.197 

3.18 

0.26 

0.  1124 

2500 

5.562 

0.8365 

0.362 

4.5 

0.575 

0.248 

3.425 

0.295 

0.1276 

•~~™~ 

20" 

.————_. 

3000 

6.674 

1.19 

0.515 

5.4 

0.79 

0.342 

4.11 

0.405 

0.175 

3.308 

0.25 

0.108 

3300 

7.34 

1.45 

0.6285 

5.94 

0.93 

0.402 

4.52 

0.475 

0.2056 

3.64 

0.294 

0.127 

3500 

7.786 

1.61 

0.697 

6.3 

1.045 

0.  452 

4.795 

0.53 

0.229 

3.86 

0.325 

0.1406 

4000 

8.898 

2.10 

0.910 

7.2 

1.445 

0.  675 

5.48 

0.68 

0.294 

4.41 

0.415 

0.  1796 

4500 

10.  0 

2.65 

1.15 

8.1 

1.67 

0.723 

6.165 

0.84 

0.363 

4.955 

0.51 

0.  2208 

5000 

11.1 

3.3 

1.43 

9. 

2.03 

0.879 

6.85 

1.02 

0.441 

5.51 

0.61 

0.264 

6000 

13.4 

4.8 

2.07 

10.8 

2.9 

1.256 

8.22 

1.425 

0.616 

6.61 

0.87 

0.3765 

7300 

13.13 

4.16 

1.804 

10. 

2.065 

0.894 

8.05 

1.24 

0.536 

7500 

B-MMOB 

30* 

13.5 

4.4 

1.905 

10.  275 

2.175 

0.94 

8.26 

1.3 

0.563 

10000 

4.77 

0.315 

0.137 

13.70 

3.67 

1.588 

11.02 

2.245 

0.972 

10500 

5.10 

0.35 

0.1515 

14.4 

4.16 

1.8 

11.58 

2.47 

1.07 

14000 
15000 

6.69 
7.16 

0.58 
0.658 

0.251 
0.284 

4.93 

36" 

0.271 

0.117 

15.43 

4.25 

1.84 

17000 

8.11 

0.845 

0.36 

5.58 

0.344 

0.149 

4O" 

20000 

9.55 

1.13 

0.489 

6.57 

0.471 

0.204 

5.28 

0.22 

0.0952 

25000 

11.94 

1.75 

0.757 

8.21 

0.71 

0.307 

6.61 

0.30 

0.1298 

_____ 

45* 

-- 

30000 

14.32 

2.473 

1.07 

9.95 

1.02 

0.441 

7.93 

0.45 

0.  1946 

6.255 

0.35 

0.1515 

35000 

11.59 

1.37 

0.593 

9.25 

0.63 

0.  2725 

7.29 

0.46 

0.199 

40000 

13.23 

1.765 

0.764 

10.59 

0.81 

0.35 

8.33 

0.585 

0.253 

45000 

14.78 

2.182 

0.944 

11.9 

1.15 

0.498 

9.37 

0.785 

0.34 

50000 

13.22 

1.6 

0.6915 

10.42 

0.90 

0.389 

60000 

12.5 

1.273 

0.551 

70000 

14.58 

1.72 

0.745 

80000 

90000 

100000 

PUMPING    MACHINERY,'  AIR 


144 


C  REEK.     MICHIGAN,     U.  S.  A. 


Table  of  Friction  of  Water  in  Pipes 

(Continued) 

.  '.>jity  in  feet  per  sec.,  the  friction  head  in  feet,  and  friction  loss  in  Ibs.  pressure  per  sq.  in 
for  each  100  feet  in  length  of  pipe,  for  different  sizes  of  clean  iron  pipe 
discharging  given  quantities  per  minute. 


Gallons  per 
minute 

Velocity 
in  feet 
per  second 

•r^rrt  <u 

o  a  & 
'££.* 

CJ§.S 

|.sj 

Us 

Velocity 
in  feet 
per  second 

c 
111 

°C  v 

foE.S 

Friction 
loss  in  Ibs. 
per  sq.  in. 

Velocity 
in  feet 
per  second  | 

a 

O       *J 

•^J 
£*.s 

Friction 
loss  in  Ibs. 
per  sq.  in. 

Velocity 
in  feet 
per  second 

a 

O       *J 

'S"S3 
B8.s 

B|3 
$** 

2J& 

2" 

2V 

5 

0.49 

0.092 

0.04 

0.244 

0.046 

0.02 

3" 

10 

0.98 

0.277 

0.12 

0.656 

0.092 

0.04 

0.448 

0.046 

0.02 

3V 

15 

1.47 

0.577 

0.25 

0.985 

0.185 

0.08 

0.672 

0.092 

0.04 

0.498 

0.046 

0.02 

20 

2.04 

0.97 

0.42 

1.315 

0.323 

0.14 

0.896 

0.138 

0.06 

0.664 

0.069 

0.03 

25 

2.6 

1.43 

0.62 

1.645 

0.485 

0.21 

1.12 

0.231 

0.10 

0.83 

0.092 

0.04 

30 

3.03 

2.09 

0.91 

1.97 

0.693 

0.30 

1.345 

0.30 

0.13 

0.996 

0.138 

0.06 

35 

3.54 

2.76 

1.22 

2.29 

0.92 

0.40 

1.569 

0.393 

Q.17 

.163 

0.208 

0.09 

40 

4.05 

3.68 

1.60 

2.62 

1.19 

0.53 

1.79 

0.53 

0.23 

.329 

0.254 

0.11 

45 

4.56 

4.60 

1.99 

2.95 

1.49 

0.66 

2.016 

0.647 

0.28 

.494 

0.323 

1.14 

50 

5.1 

5.61 

2.44 

3.3 

1.86 

0.81 

2.24 

0.80 

0.35 

.66 

0.393 

0.17 

60 

6.12 

8.88 

3.50 

3.95 

2.7 

1.17 

2.688 

1.155 

0.50 

.992 

0.555 

0.24 

70 

7.14 

11.09 

4.80 

4.6 

3.46 

1.50 

3.136 

1.385 

0.60 

2.324 

0.879 

0.38 

75 

7.7 

12.23 

5.32 

4.93 

4.14 

1.80 

3.360 

1.70 

0.75 

2.490 

0.913 

0.395 

80 

8.16 

14.55 

6.30 

5.26 

4.62 

2.00 

3.584 

2.08 

0.90 

2.656 

0.948 

0.41 

90 

9.18 

18.02 

7.80 

5.91 

5.96 

2.58 

4.032 

2.54 

1.10 

2.988 

1.247 

0.54 

100 

10.2 

21.75 

9.46 

6.5 

7.36 

3.20 

4.480 

3.01 

1.31 

3.320 

1.478 

0.64 

125 

12.8 

34.27 

14.9 

8.13 

11.24 

4.89 

5.6 

4.57 

1.99 

4.15 

2.219 

0.96 

150 

15.3 

48.76 

21.2 

9.8 

16.10 

7.00 

6.8 

6.55 

2.85 

4.98 

3.12 

1.35 

175 

11.43 

21.75 

9.46 

7.92 

8.85 

3.85 

5.81 

4.208 

1.82 

185 

11.84 

24.5 

10  .'61 

8.34 

9.94 

4.3 

6.14 

4.62 

2.00 

200 

- 

8" 

• 

13.06 

28.86 

12.47 

9.04 

11.54 

5.02 

6.64 

5.50 

2.38 

'     250 

1.6 

0.162 

0.07 

11.28 

17.84 

7.76 

8.30 

8.55 

3.70 

265 

1.698 

0.175 

0.0757 

9" 

12.4 

20.09 

8.72 

8.8 

9.6 

4.15 

300 

1.9 

0.208 

0.09 

1.5 

0.115 

0.05 

13.52 

25.76 

11.2 

9.96 

11.63 

5.04 

350 

2.2 

0.2775 

0.12 

1.75 

0.1618 

0.07 

11.62 

16.4 

7.10 

370 

2.37 

0.306 

0.1324 

1.85 

0.178 

0.077 

12.  28 

18.13 

7.85 

400 
450 

2.6 
2.92 

0.37 
0.462 

0.16 
0.20 

2. 
2.25 

0.208 
0.2545 

0.09 
0.11 

1.8 

1O" 

0.1618 

0.07 

13.28 

21.36 

9.25 

480 

3.07 

0.498 

0.2155 

2.4 

0.3 

0.13 

1.92 

1.1816 

0.  0785 

12" 

—  — 

500 

3.2 

0.5785 

0.25 

2.5 

0.324 

0.14 

2. 

0.204 

0.09 

1.4 

0.0925 

0.04 

750 

4.8 

1.224 

0.53 

3.75 

0.6945 

0.30 

3. 

0.416 

0.18 

2.1 

0.1848 

0.08 

1000 

6.4 

2.17 

0.94 

5. 

1.224 

0.53 

4. 

0.74 

0.32 

2.8 

0.304 

0.13 

1100 

7.04 

2.64 

1.142 

5.5 

1.50 

0.649 

4.4 

0.88 

0.381 

3.08 

0.375 

0.162 

1200 

8.0 

3.378 

1.46 

6.25 

1.895 

0.82 

5. 

1.132 

0.49 

3.5 

0.462 

0.20 

1550 

9.6 

4.84 

2.09 

7.5 

2.704 

1.17 

6.1 

1.618 

0.70 

4.2 

0.67 

0.29 

2000 

12.7 

8.70 

3.765 

8.1 

2.842 

1.23 

5.6 

1.132 

0.49 

2200 

14.09 

10.71 

4.64 

8.8 

3.34 

1.446 

6.16 

1.38 

0.598 

2500 

10.1 

4.43 

1.92 

7. 

1.78 

0.77 

3000 

22" 

12.1 

5.30 

2.725 

8.4 

2.567 

1.11 

3300 

2.973 

0.18 

0.078 

13.2 

7.50 

3.24 

9.24 

3.08 

1.333 

3500 
4000 

3.15 
3.6 

0.20 
0.255 

0.0865 
0.114 

3.08 

24" 

0.175 

0.0758 

14.1 

8.52 
26" 

3.68 

9.8 
11.3 

4.18 
4.45 

1.81 
1.925 

4500 

4.06 

0.375 

0.162 

3.47 

0.223 

0.0965 

2.874 

0.14 

0.0606 

12.75 

5.55 

2.4 

5000 

4.5 

0.40 

0.173 

3.855 

0.27 

0.117 

3.19 

0.22 

0.0952 

14.0 

6.65 

2.88 

6000 

5.4 

0.55 

0.234 

4.62 

0.375 

0.162 

3.815 

0.241 

0.104 

28" 

7300 

6.57 

0.78 

0.337 

5.625 

0.53 

0.229 

4.658 

0.35 

0.1515 

4.015 

0.235 

0.1019 

7500 

6.75 

0.825 

0.357 

5.783 

0.56 

0.232 

4.785 

0.363 

0.157 

4.125 

0.252 

0.1092 

10000 

9. 

1.392 

0.633 

7.708 

0.94 

0.4065 

6.38 

0.62 

0.2685 

5.5 

0.43 

0.186 

10500 

9.45 

1.53 

0.663 

8.1 

1.03 

0.445 

6.7 

0.68 

0.2944 

5.77 

0.475 

0.26 

14000 

12.6 

2.64 

1.142 

10.79 

1.792 

0.776 

8.93 

1.15 

0.498 

5.7 

0.82 

0.3555 

15000 

13.5 

3.01 

1.304 

11.56 

2.05 

0.888 

9.57 

1.305 

0.565 

8.25 

0.93 

0.405 

17000 

15.3 

3.8 

1.645 

13.10 

2.6 

1.125 

10.84 

1.66 

0.729 

9.35 

1.17 

0.56 

20000 

15.4 

3.52. 

1.524 

12.76 

2.125 

0.97 

11.00 

1.6 

0.693 

25000 

13.75 

2.45 

1.062 

30000 

35000 
40000 

6.76 

50" 

0.358 

0.155 

5.56 

55  " 

0.226 

0.081 

60" 

45000 

7.605 

0.446 

0.193 

6.25 

0.281 

0.1216 

5.245 

0.187 

0.0809 

50000 

8.45 

0.544 

0.235 

6.94 

0.345 

0.1492 

5  825 

0.226 

0.0977 

60000 

10.14 

0.766 

0.332 

8.43 

0.4915 

0.2343 

6.99J 

0.319 

0.1382 

70000 

9.82 

0.655 

0.2835 

8.155 

0.422 

0.1828 

80000 

11.21 

0.8292 

0.358 

9.320 

0.548 

0.2356 

90000 

10.485 

0.682 

0.295 

J  00000 

11.650 

0.83 

0.359 

AND    CONDENSERS    FOR   EVERY  SERVICE 


145 


Friction  in  Elbows 


O  o. 

[|1 

i 

Friction 
loss  in  Ibs. 
per  so.  in. 

Velocity 
in  feet 
per  sec. 

c  c 

III 

111 

Velocity 
in  feet 
per  sec. 

PH  1—  <  <-£4 

Friction 
loss  in  Ibs. 
per  sq.  in. 

lisfc 

g.8 

H« 

Friction 
loss  in  Ibs. 
per  sq.  in.  || 

5 

3.64 

0.161 

0.07 

2.04 

0.0624 

0.027 

1.3 

U" 

0.0185 

0.008 

14" 

10 

7.28 

0.644 

.28 

4.08 

0.217 

0.094 

2.6 

0.0716 

0.031 

15 

0.92 

1.449 

0.63 

6.12 

0.488 

0.212 

3.9 

0.1592 

0.069 

2.73 

0.092 

0.04 

20 

4.56 

2.576 

1  12 

8.16 

0.8675 

0.376 

5.2 

0.2835 

0.123 

3.64 

0.1591 

0.069 

25 

8.2 

4.002 

1.74 

10.20 

1.35 

0.585 

6.5 

0.448 

0.194 

4.55 

0.249 

0.108 

30 

12.24 

1.95 

0.845 

7.8 

0.642 

0.278 

5.46 

0.362 

0.157 

35 

4" 

• 

14.28 

2.65 

1.15 

9.1 

0.877 

0.380 

6.37 

0.495 

0.215 

40 

1.04 

0.01614 

0.007 

16.  32 

3.46 

1.5 

10.4 

1.143 

0.495 

7.28 

0.641 

0.278 

45 

1.17 

0.0208 

0.009 

11.7 

1.445 

0.626 

8.19 

0.81 

0.352 

50 
00 

1.3 
1.56 

0.  0231 
0.0345 

0.01 
0.015 

0.88 

5" 
0.01382 

0.006 

13. 
15.6 

1.778 
2.562 

0.77 
1.11 

9.1 

10.92 

0.99 
1.429 

0.43 
0.62 

70 

1.82 

0.0485 

0.021 

1.04 

0.0208 

0.009 

18.2 

3.51 

1.52 

12.74 

1.82 

0.86 

75 

1.95 

0.0552 

0.024 

1.2 

0.0231 

0.01 

19.5 

4.02 

1.74 

13.65 

2.26 

0.98 

80 

2.08 

0.0623 

0.027 

1.28 

0.0277 

0.012 

20.8 

4.57 

1.98 

14.56 

2.56 

1.11 

90 

2.34 

0.0808 

0.035 

1.44 

0.0323 

0.014 

—  —  ^ 

6" 

16.38 

3.25 

1.41 

100 

2.60 

0.0992 

0.043 

1.6 

0.0392 

0.017 

1.14 

0.01845 

0.008 

"^^^^^ 

125 

3.25 

0.1546 

0.067 

2. 

0.  0622 

0.027 

1.42 

0.03 

0.013 

7" 

150 

3.8 

0.2215 

0.096 

24 

0.09 

0.039 

1.71 

0.0438 

0.019 

1.2 

0.0231 

0.01 

175 

4.45 

0.3048 

0.132 

2.8 

0.  1222 

0.053 

2. 

0.06 

0.026 

1.38 

Ois2b 

0.010 

185 

4.7 

0.348 

0.  1509 

2.96 

0.1342 

0.0582 

2.11 

0.068 

0.0294 

1.55 

0^349 

0.0149 

200 

5.1 

0.397 

0.172 

3.2 

0.157 

0.068 

2.28 

0.0738 

0.032 

1.7 

0.046'2 

0.02 

250 

6.4 

0.6195 

0.268 

4. 

0  252 

0.109 

2.8 

0.11967 

0.  0518 

2.1 

0.0669 

0.029 

265 

6.79 

0.7025 

0.34 

4.24 

0.2743 

0.119 

3.03 

0.14U4 

0.067 

2.23 

0.076 

0.0339 

300 

7.6 

0.886 

0.384 

4  8 

0.36 

0.156 

3.4 

0.1754 

0.076 

2.4 

0.09()9 

0.042 

350 

8.9 

1.244 

0.530 

5.6 

0  496 

0.215 

3.9 

0.2375 

0.103 

2.94 

0.1314 

0.057 

370 

9.41 

1.35G 

0.587 

5.92 

0.535 

0.232 

4.22 

0.273 

0.1182 

3.1 

0.149 

0.0645 

400 

10.1 

1.586 

0.688 

6.5 

0.6275 

0.2/2 

4.5 

0.295 

0.128 

3.36 

0.1845 

0.08 

450 

11.4 

2.015 

0.8/0 

7.3 

0.811 

0.352 

5.05 

0.392 

0.170 

3.96 

0.217 

0.094 

480 

12.16 

2.256 

0.9/6 

7.68 

0  901 

0.39 

5.49 

0.4602 

0.  1994 

4.03 

0.2454 

0.1062 

500 

12.7 

2.47 

1.07 

8.1 

1.007 

0.436 

5.6 

0.481 

0.208 

4.2 

0.2b,o 

0.  116 

75'J 
1000 

2.224 

14" 

0.0772 

0.  0335 

12.1 
16.1 

2.24 
4.02 

0.9/0 
1.74 

8.4 
11.3 

1.085 
1.92 

0.470 
0.832 

6.3 

8.4 

0.6 
1.069 

U.  260 
0.464 

1100 

2.444 

0.0917 

0.039V 

12.57 

2.413 

1.045 

9.25 

1.329 

0.575 

1250 

2.78 

0.  1185 

0.0517 

——  —  —  . 

15" 

14.1 

3.025 

1.31 

10.  5 

1.676 

0.  '/28 

1500 

3.336 

0.1695 

0.  0738 

2.7 

0.112 

0.  0486 

18" 

12.6 

1.938 

0.84 

2000 

4.448 

0.303 

0.131 

3.6 

0.1985 

0.0859 

2.74 

0.115 

0.  0498 

2200 

4.9 

0.367 

0.159 

3.96 

0.249 

0.108 

3.18 

0.1548 

0.066 

2500 

5.562 

0.475 

0.206 

4.5 

0.311 

0.1347 

3.425 

0.1795 

0.0779 

- 

20" 

™  ™""* 

3000 

6.674 

0.690 

0.3 

5.4 

0.4485 

0.  1944 

4.11 

0.258 

0.112 

3.308 

0.168 

0.073 

3300 

7.34 

0.8215 

0.353 

5.94 

0.539 

0.233 

4.52 

0.313 

0.  1357 

3.64 

0.203 

0.0883 

3500 

7.786 

0.927 

0.  402 

6.3 

0.609 

0.264 

4.795 

0.352 

0.  1525 

3.86 

3.228 

0.0992 

4000 

8.898 

1.206 

0.526 

7.2 

0.795 

0.3435 

5.48 

0.462 

0.2 

4.41 

0.298 

0.0998 

4500 

10.013 

1.539 

0.665 

8.1 

1.016 

0.442 

6.165 

0.583 

0.253 

4.955 

0.378 

0.164 

5000 

12.237 

2.29 

0.997 

9. 

1.243 

0.5395 

6.85 

0.719 

0.312 

5.51 

0.4675 

0  232 

6000 

14.461 

3.22 

1.39 

10.8 

1.79 

0.774 

8.22 

1.03 

0.447 

6.61 

0.671 

0.292 

730) 

13.13 

2.639 

1.143 

10. 

1.555 

0.674 

8.05 

0.984 

3.4275 

7500 
10000 

4.77 

30" 

0.35 

0.152 

13.5 

2.798 

1.212 

10.275 
13.70 

1.615 

2.88 

0.701 
1.25 

8.26 
11.02 

1.048 
1.87 

0^814 
0  '111 

10500 
14000 

5.10 
6.69 

0.3995 
0.686 

0.1735 
0.298 

36" 

14.4 
19. 

3.18 
5.64 

1.378 
2.44 

LI.  58 
15.43 

2.095 
3.67 

j.  j  1  1 
1.595 

15000 

7.16 

0.778 

0.338 

4.93 

0.374 

0.162 

20.55 

6.49 

2.81 

17000 

8.11 

•  1.246 

1.591 

5.58 

0.4765 

0.2063 

20000 

9.55 

1.40 

0.609 

6.57 

0.662 

0.287 

- 

40" 

«—  — 

25000 

11.94 

2.188 

0.948 

8.21 

1.034 

0.448 

6.61 

0.669 

0.29 

_^_  — 

45" 

^""^^ 

goooo 

14.32 

3.15 

1.37 

9.95 

1.515 

0.656 

7.93 

0.963 

0.417 

6.255 

0.6 

0.26 

35000 

11.59 

2.06 

0.892 

9.25 

1.312 

0.568 

7.29 

0.416 

0.3525 

40000 

13.23 

2  68 

1.164 

10.57 

1.71 

0.7395 

8.33 

1.031 

0.46 

45000 

14.87 

3.39 

1.467 

11.89 

2  17 

0.94 

9.37 

1.349 

0  585 

50000 

16.51 

4.19 

1.815 

13.21 

2.68 

1.161 

10.41 

1.669 

0.721 

60000 

19.80 

6.04 

2.62 

15.85 

3.85 

1.665 

12.495 

2.39 

1.035 

70000 

23.  09 

8  19 

3.55 

18.49 

5.25 

2.275 

14.58 

3.25 

1.41 

8000( 

26  38 

10.64 

4.62 

22.18 

7.53 

3.26 

16.665 

4.26 

1.85 

90000 

29.67 

13.5 

5.85 

24.77 

9.44 

4.09 

18.75 

5.39 

2.34 

100000 

32.96 

16.62 

7.41 

27  41 

11.52 

5.00 

20.835 

6.68 

2.89 

NOTE — Calculated  from  Weisback's  formula  for  very  short  bends  with  a  radius  equal 
to  the  radius  of  the  pipe. 


i           * 

ATTLE 

C 

RE 

EK 

M 

ICHIG 

AN, 

U. 

S. 

A. 

3 

Friction  in  Elbows 

(Continued) 


Velocity  (1 
in  feet 
per  sec. 

«  c 

111 

Friction  1 
lossinlbs. 
per  sq.  in. 

>> 

i«s 
IH 

& 

s&* 

•ISJ 

•c  8fc 
fc.S  a 

tli 
£51 

s  s 

o 
'+3-T3 
0  aj  ,-> 

•r  aj  <u 

£K£ 

Jfi 

ii^ 

fc.2  a 

JM 

c  c 

O—1 

°+3-a 

o  rt  -w 

'&£$ 

CJ3.£ 
•& 

£|g 

|! 

'S  £ 
0  a 

5 

10 

15 

2a 

20 

2.6 

0.087 

0.038 

25 

3.03 

0.127 

0.055 

2i" 

30 

3.54 

0.1755 

0.076 

2.29 

0.0854 

0.037 

35 

4.05 

0.  2264 

0.098 

2.62 

0.  1131 

0.049 

3" 

40 

4.56 

0.288 

0.125 

2.95 

0.143 

0.062 

2.016 

0.0599 

0.026 

45 

5.1 

0.353 

0.153 

3.3 

0.  1848 

0.08 

2.24 

0.0738 

0.032 

3i" 

50 

6.12 

0.5075 

0.22 

3.95 

0.258 

0.112 

2.688 

0.  1015 

0.044 

1.992 

0.06 

0.026 

60 

7.14 

0.701 

0.304 

4.6 

0.3415 

0.148 

3.136 

3.  1383 

0.06 

2.324 

0.0808 

0.035 

70 

7.7 

0.808 

0.35 

4.93 

0.397 

0.172 

3.360 

0.166 

0.072 

2.490 

0.0923 

0.04 

75 

8.16 

0.925 

0.392 

5.26 

0.452 

0.196 

3.584 

0.  1845 

0.08 

2.656 

0.1014 

0.044 

80 

9.18 

1.155 

0.5 

5.91 

0.573 

0.248 

4.032 

0.2395 

0.104 

2.988 

0.  1385 

0.06 

90 

10.2 

1.412 

0.612 

6.5 

0.738 

0.32 

4.480 

0.295 

0.128 

3.320 

0.1569 

0.068 

100 

12.8 

2.24 

0.97 

8.13 

1.175 

0.48 

5.6 

0.462 

0.2 

4.15 

0.258 

0.112 

125 

15.3 

3.205 

1.39 

9.8 

1.58 

0.685 

6.8 

0.659 

0.286 

4.98 

0.  3695 

0.16 

150 

11.43 

2.16 

0.935 

7.92 

0.899 

0.390 

5.81 

0.504 

0.218 

175 

1.84 

2.42 

1.049 

8.34 

L.055 

0.457 

6.14 

0.5745 

0.248 

185 

1.6 

8* 
0.0392 

0.017 

3.06 

2.955 

1.28 

9.04 
11.28 

1.18 
L.845 

0.512 
0.8 

6.64 
8.30 

).628 
1.029 

0.272 
0.446 

200 
250 

1.698 
1.9 

3.044] 
0.0577 

0.191 
0.025 

1.5 

9" 

0.0369 

0.016 

12.4 
13.52 

2.35 
2.63 

1.018 
1.14 

8.8 
9.96 

L.183 
1.478 

).513 
0.64 

265 
300 

2.2 

0.0784 

0.034 

1.75 

0.0507 

0.022 

1.62 

2.03 

0.88 

350 

2.37 

0.0843 

0.365 

1.85 

0.0573 

0.0248 

2.28 

2.302 

0.997 

370 

2.6 

0.1015 

0.044 

2. 

0.0646 

0.028 

10" 

3.28 

2.515 

1.09 

400 

2.92 

0.1315 

0.057 

2.25 

0.083 

0.036 

1.8 

0.053 

0.023 

450 

3.07 

0.144 

0.  0624 

2.4 

0.088 

0.038 

1.92 

0.0563 

0.  0244 

12" 

480 

3.2 

0.1568 

0.068 

2.5 

0.1015 

0.044 

2.  ' 

0.065 

0.028 

1.4 

0.  0369 

0.016 

500 

4.8 

0.3598 

0.156 

3.75 

0.231 

0.102 

3. 

0.1453 

0.063 

2.1 

0.0715 

0.031 

750 

6.4 

0.627 

0.272 

5. 

0.406 

0.176 

4. 

0.258 

0.112 

2.8 

0.1439 

0.064 

1000 

7.04 

0.756 

0.  3295 

5.5 

0.4615 

0.2 

4.4 

0.293 

0.127 

3.08 

0.145 

0.  6028 

1100 

8.0 

1.005 

0.435 

6.25 

0.637 

0.276 

5. 

0.403 

0.175 

3.5 

0.1981 

0.086 

1250 

9.6 

1.44 

0.624 

7.5 

0.923 

0.4 

6.1 

0.58 

0.252 

4.2 

0.286 

124 

1500 

12.7 

2.44 

1.055 

10. 

1.535 

0.665 

8.1 

1.008 

0.436 

5.6 

0.4747 

.205 

2000 

14.09 

3.025 

1.308 

11. 

1.85 

0.815 

8.8 

1.183 

0.513 

6.16 

0.5805 

.2518 

2200 

15.9 

3.88 

1.68 

2.5 

2.395 

1.035 

10.1 

1.568 

0.68 

7. 

0.752 

.327 

2500 

5. 

3.46 

1.5 

12.1 

2.248 

0.975 

8.4 

1.082 

.429 

3000 

22" 

13.2 

2.63 

1.14 

9.24 

1.34 

.5802 

3300 

3.15 
3.6 

0.  1525 
0.1992 

0.  0664 
0.0867 

3.08 

24:" 

0.146 

0.0685 

14.1 

3.05 

1.325 

9.8 
1.92 

1.471 
1.92 

.638 
.833 

3500 
4000 

4.06 

0.253 

1.10 

3.47 

0.1873 

0.  0815 

2.6 

2.435 

.055 

4500 

4.5 

0  312 

0  1344 

3.855 

0.2285 

0.0994 

4. 

3.01 

.34 

5000 

5.4 

0.0448 

0.194 

4.62 

0.  3288 

0.143 

6000 

6.57 

0.66 

0.286 

5.625 

0.486 

0.2112 

7310 

6.75 

0.698 

0.303 

5.783 

0.564 

0.245 

26" 

7500 

9. 

1.241 

0.539 

7.708 

0.912 

0.396 

6.38 

.625 

0.271 

10000 

9.45 

1.36 

0.589 

8.1 

1.01 

0.4385 

6.7 

0.6866 

0.297 

10500 

12.6 

2.578 

1.117 

0.79 

1.788 

0.777 

8.93 

.223 

0.53 

_—  «~ 

28" 

» 

14000 

13.5 

2.8 

1.212 

1.56 

2.05 

0.891 

9.57 

.408 

0.609 

8.25 

.09 

.472 

15000 

15.3 

3.568 

1.546 

3.10 

2.64 

1.147 

0.84 

.95 

0.845 

9.35 

.334 

.578 

17000 

18. 

4.96 

2.15 

5.4 

3.64 

1.58 

12.  76 

.49 

1.084 

1.00 

.855 

.806 

20000 

22.5 

7.76 

3.355 

7.05 

.47 

1.939 

3.75 

.945 

.208 

25000 

0.24 

6.18 

2.68 

6.50 

4.16 

.802 

30000 

6.76 

50" 

0.680 

0.295 

5.56 

55° 

0.475 

0.206 

25.52 

.98 

4.32 

9.25 
2.00 

5.68 
.43 

.46 
.225 

35000 
40000 

7.605 
8.45 

).890 
1.095 

0.385 
0.475 

6.25 
6.94 

0.599 
0.730 

0.259 
0.316 

5.825 

60" 

.52 

0.'226 

4.75 

27.50 

.89 
1.6 

.07 
.2 

45000 
50000 

10.14 

.157 

0.680 

8.43 

.09 

0.473 

6.790 

.749 

0.324 

60000 

11.83 

2.14 

0.930 

9.82 

.48 

0.642 

8.155 

.02 

0.4425 

70000 

13.52 

2.81 

1.215 

1.21 

.93 

0.833 

9.320 

.33 

0.575 

80000 

15.21 

3.56 

1.54 

2.60 

2.43 

1.055 

0.485 

.7 

0.735 

)0000 

16.90 

4.4 

1.91 

3.99 

3.00 

1.300 

11.650 

.08 

0.91 

00000 

NOTE — Calculated  from    Weisback's  formula  for  very  short  bends  with  a  radius  equal 
to  the  radius  of  the  pipe. 


AND 


147 


jj        UN 

I  ON 

STEAM 

P  UM  P 

C  O  MPANV 

il 

Friction  of  Standard  Pipe  Fittings 

The  following  equivalent  length  of  straight  pipe  snould  be 
added  for  each  fitting  in  figuring  friction : 
Size  of 

1       IX       IK       2       2K       3       4       5       6 
56  7  7     10         12     IS     25     30 

10     12         14         11     20         24     36     50     60 
67  8  8     12,       24     30     40     50 


Fittings K 

Elbows 5 

Return  Bends  10 
Globe  Valves..  6 


Owing  to  the  burr  (caused  by  cutting  the  pipe  with  wneel 
cutter)  obstructing  the  flow  in  the  smaller  pipes,  it  is  advisable, 
unless  the  burrs  are  reamed  out,  to  multiply  the  above  figures, 
by  3  for  ^  and  1  inch  fittings  and  by  2  for  !><>  IK  and  2  inch 
fittings. 

Equation  of  Pipes 

The  following  table  gives  the  actual  dimensions  of  standard 
"Merchant"  wrought  iron  pipe  with  the  inside  diameter  in  inches 
of  each  branch  in  a  series  of  equal  branches,  whose  total  internal 
cross  sectional  area  is  equal  to  that  of  the  main  pipe.  Thus  if 
it  is  desired  to  find  the  size  of  pipe  required  for  four  branches, 
whose  internal  cross  sectional  area  is  equal  to  that  of  a  3  inch 
pipe,  by  referring  to  the  table  opposite  the  3  inch  pipe  and  under 
4,  the  diameter  1.533  inches  is  found,  which  is  the  required  di- 
mension. By  reference  to  the  column  of  diameters,  it  will  be 
seen  that  the  proper  size  of  pipes  will  be  IX  inches,  the  diameter 
of  this  size  being  1.611  inches.  No  account  of  friction  is  taken 
in  this  table,  which  must  be  considered  in  any  actual  problem. 


Actual  Inter- 

Actual 

Diameter  in  inches  of  each  branch  of  the  following 

1 

nal  Area 

Diam. 

number  of  equivalent  branches 

1 

£ 

I 

Square 

Square 

Inches 

2 

3 

4 

5 

6 

7 

8 

9 

10 

£ 
§ 

02 

Inches 

Feet 

cc 

.0568 

.0004 

.27 

.1041 

.0007 

.364 

'   '.257 

'"210 

.1909 

.0013 

.484 

.349 

.285 

.247 

.220 

.3039 

.0021 

.623 

.440 

.359 

.311 

.279 

.254 

.231 

.220 

.207 

.5333 

.0037 

.824 

.582 

.475 

.412 

.368 

.336 

.311 

.291 

.274 

'"260 

1 

.8609 

.0060 

1.048 

.741 

.605 

.524 

.468 

.427 

.400 

.375 

.349 

.331 

j 

H 

1.4957 

.0104 

1.380 

.976 

.796 

.690 

.617 

.563 

.521 

.488 

.460 

.436 

li 

li 

2.036 

.0141 

1.611 

1.139 

.930 

.805 

.720 

.657 

.608 

.570 

.537 

.594 

l] 

2 

3.356 

.0233 

2.067 

1.461 

1.193 

1.033 

.924 

.843 

.781 

.730 

.689 

.653 

2 

2i 

4.780- 

.0332 

2.468 

1.745 

1.424 

1.234 

1.103 

1.007 

.932 

.872 

.822 

.780 

2i 

3 

7.383 

.0513 

3.067 

2.169 

1.770 

1.533 

1.372 

1.252 

1.159 

1.084 

1.022 

.970 

3 

3i 

9.886 

.0687 

3.548 

2.509 

2.048 

1.774 

1.586 

1.448 

1.340 

1.253 

1.182 

1.123 

3J 

4 

12.730 

.0884 

4.026 

2.847 

2.330 

2.013 

1.809 

1.643 

1.521 

1.423 

1.342 

1.273 

4 

4i 

15.961 

.1108 

4.508 

3.185 

2.602 

2.254 

2.016 

1.840 

1.703 

1.594 

1.502 

1.425 

4i 

5 

19.986 

.1388 

5.045 

3.568 

2.912 

2.522 

2.256 

2  059 

1.906 

1.784 

1.681 

1.595 

5 

6 

28.886 

.2006 

6.065 

4.289 

3.501 

3.032 

2.716 

2.475 

2.292 

2.144 

2.021 

1.918 

6 

7 

38.  743 

.2690 

7.023 

4.966 

4.054 

3.511 

3.140 

2.867 

2.654 

2.483 

2.341 

2.228 

7 

8 

50.021 

.3474 

7.982 

5.645 

4.618 

3.991 

3.570 

3.258 

3.013 

2.822 

2.661 

2.524 

8 

10 

78.822 

.5474 

10.019 

7.085 

5.785 

5.009 

4.462 

4.090 

3.783 

3.603 

3.339 

3.168 

10 

12 

113.088 

.7854 

12.000 

8.486 

6.928 

6.000 

5.367 

4.898 

4.635 

4.243 

4.000 

3.794 

12 

14 

159.485 

1.1075 

13.250 

9.370 

7.650 

6.625 

5.926 

5.409 

5.007 

4.684 

4.410 

4.189 

14 

I 


utJ 


148 


Theoretical  Discharge  of  Nozzles  in  U.  S. 
Gallons  per  Minute 


Head 

&i 

DIAMETER  OF  NOZZLE  IN  INCHES 

Lbs 

.'Feet 

J>1* 
£Q£. 

A 

i 

& 

1 

* 

1 

f 

I 

1 

1 

U 

11 

H 

IF 

23.1 

38.6 

0.37 

1~48 

3.32 

5.91 

13~3 

23.6 

36.9 

53.1 

72.4 

94.5 

120 

148 

179 

15 

34.6 

47.25 

0.45 

LSI 

4.06 

7.24 

16.3 

28.9 

45.2 

65.0 

88.5 

116. 

147 

181 

219 

20 

46.. 

54.55 

0.52 

2.09 

4.69 

8.35 

18.  S 

33.4 

52.2 

75.1 

102. 

134. 

169 

209 

253 

25 

57.7 

61.0 

0.58 

2.34 

5.25 

9.34 

21.0 

37.3 

53.3 

84.0 

114. 

149. 

189 

234 

283 

30 

69.3 

66.85 

0.64 

2.56 

5.75 

K>.2 

23.0 

40.9 

(.3.9 

92.0 

125. 

164. 

207 

256 

309 

35 

80.8 

72.2 

0.69 

2.77 

6.21 

11.1 

24.8 

44.2 

69.0 

99.5 

135. 

177. 

224 

277 

334 

40 

92.4 

77.2 

0.74 

2.96 

6.64 

11.8 

26.6 

47.3 

73.8 

106. 

145. 

189. 

239 

296 

357 

45 

103.9 

81.8 

0.78 

3.13 

7.03 

12.5 

28.2 

50.1 

78.2 

113. 

153. 

200. 

253 

313 

379 

50 

115.5 

86.25 

0.83 

3.30 

7.41 

13.2 

29.7 

52.8 

82.5 

119. 

162. 

211. 

267 

330 

399 

55 

127.0 

90.4 

0.87 

3.46 

7.77 

13.8 

31.1 

55.3 

86.4 

125. 

169. 

221. 

280 

346 

418 

60 

138.6 

94.5 

0.90 

3.62 

8.12 

14.5 

32.5 

57.8 

90.4 

130. 

177. 

231. 

293 

362 

438 

65 

150.1 

98.3 

0.94 

3.77 

8.45 

15.1 

33.8 

60.2 

94.0 

136. 

184. 

241. 

305 

376 

455 

70 

161.7 

102.1 

0.98 

3.91 

8.78 

15.7 

35.2 

62.5 

97.7 

141. 

191. 

250. 

317 

391 

473 

75 

173.2 

105.7 

1.01 

4.05 

9.08 

16.2 

36.4 

64.7 

101. 

146. 

198. 

259. 

327 

404 

489 

80 

184.8 

109.1 

1.05 

4.18 

9.39 

16.7 

37.6 

66.8 

104. 

150. 

205. 

267. 

338 

418 

505 

85 

196.3 

112.5 

1.08 

4.31 

9.67 

17.3 

38.8 

68.9 

108. 

155. 

211. 

276. 

349 

431 

521 

90 

207.9 

115.8 

1.11 

4.43 

9.95 

17.7 

39.9 

70.8 

111. 

160. 

217. 

284. 

359 

443 

536 

95 

219.4 

119.0 

1.14 

4.56 

10.2 

18.2 

41.0 

72.8 

114. 

164. 

223. 

292. 

369 

456 

551 

100 

230.9 

122.0 

1.17 

4.67 

10.5 

18.7 

42.1 

74.7 

117. 

168. 

229. 

299. 

378 

467 

565 

105 

242.4 

125.0 

1.20 

4.79 

10.8 

19.2 

43.1 

76.5 

120. 

172. 

234. 

306. 

388 

479 

579 

110 

254.0 

128.0 

1.23 

4.90 

11.0 

19.6 

44.1 

78.4 

122. 

176. 

240. 

314. 

397 

490 

593 

115 

265.5 

130.9 

1.25 

5.01 

11.2 

20.0 

45.1 

80.1 

125. 

180. 

245. 

320. 

406 

501 

606 

120 

277.1 

133.7 

1.28 

5.12 

11.5 

20.5 

46.0 

81.8 

128. 

184. 

251. 

327. 

414 

512 

619 

125 

288.6 

136.4 

1.31 

5.22 

11.7 

20.9 

47.0 

83.5 

130. 

188. 

256. 

334. 

423 

522 

632 

130 

300.2 

139.1 

1.33 

5.33 

12.0 

21.3 

48.0 

85.2 

133. 

192. 

261. 

341. 

432 

533 

645 

135 

311.7 

141.8 

1.36 

5.43 

12.2 

21.7 

48.9 

86.7 

136. 

195. 

266. 

347. 

439 

543 

656 

140 

323.3 

144.3 

1.38 

5.53 

12.4 

22.1 

49.8 

88.4 

138. 

199. 

271. 

354. 

448 

553 

668 

145 

334.8 

146.9 

1.41 

5.62 

12.6 

22.5 

50.6 

89.9 

140. 

202. 

275. 

360. 

455 

562 

680 

150 

346.4 

149.5 

1.43 

5.72 

12.9 

22.9 

51.5 

•91.5 

143. 

206. 

280. 

366. 

463 

572 

692 

175 

404.1 

161.4 

1.55 

6.18 

13.9 

24.7 

55.6 

98.8 

154. 

222. 

302. 

395. 

500 

618 

747 

200 

461.9 

172.6 

1.65 

6.61 

14.8 

26.4 

59.5 

106. 

165. 

238. 

323. 

423. 

535 

660 

799 

250 

577.4 

193.0 

1.85 

7.39 

16.6 

29.6 

66.5 

118. 

185. 

266. 

362. 

473. 

598 

739 

894 

300 

692.8 

211.2 

2.02 

8.C8 

18  2 

32.4 

72.8 

129. 

202. 

291. 

396. 

517. 

655 

808 

977 

Head 

^< 

DIAMETER  OF  NOZZLE  IN  INCHES 

Lbs 

Feet 

o-a  en 

111 

11 

II 

2 

2i 

2* 

21 

3 

31 

4 

4* 

5 

si 

6 

10 

23.1 

38.6 

213 

289 

378 

479 

591 

714 

851 

1158 

1510 

1915 

2365 

2855 

3405 

15 

34.6 

47.25 

260 

354 

463 

585 

723 

874 

1041 

1418 

1850 

2345 

2890 

3490 

4165 

20 

46.2 

54.55 

301 

409 

535 

676 

835 

1009 

1203 

1638 

2135 

2710 

3340 

4040 

4810 

25 

57.7 

61.0 

336 

458 

598 

756 

934 

1128 

1345 

1830 

2385 

3025 

3730 

4510 

5380 

30 

69.3 

66.85 

368 

501 

655 

828 

1023 

1236 

1473 

2005 

2615 

3315 

4090 

4940 

5895 

35 

80.8 

72.2 

398 

541 

708 

895 

1106 

1335 

1591 

2168 

2825 

3580 

4415 

5340 

6370 

40 

92.4 

77.2 

425 

578 

756 

957 

1182 

1428 

1701 

2315 

3020 

3830 

4725 

5710 

6810 

45 

103.9 

81.8 

451 

613 

801 

1015 

1252 

1512 

1802 

2455 

3200 

4055 

5000 

6050 

7210 

50 

115.5 

86.25 

475 

647 

845 

1070 

1320 

1595 

1900 

2590 

3375 

4275 

5280 

6380 

7600 

55 

127.0 

90.4 

498 

678 

886 

1121 

1385 

1671 

1991 

2710 

3540 

4480 

5530 

6690 

7970 

60 

138.6 

94.5 

521 

708 

926 

1172 

1447 

1748 

2C85 

2835 

3700 

4685 

5790 

6980 

8330 

65 

150.1 

98.3 

542 

737 

964 

1220 

1506 

1819 

2165 

2950 

3850 

4875 

6020 

7270 

8670 

70 

161.7 

102.1 

563 

765 

1001 

1267 

1565 

18S8 

2250 

3065 

4000 

5060 

6250 

7560 

9000 

75 

173.2 

105.7 

582 

792 

1037 

1310 

1619 

1955 

2330 

3170 

4135 

5240 

6475 

7820 

9320 

80 

184.8 

109.1 

602 

818 

1070 

1354 

1672 

'20211 

2405 

3280 

4270 

5410 

6690 

8080 

9630 

85 

196.3 

112.5 

620 

844 

1103 

139b 

1723 

2(180 

2480 

3375 

4400 

5575 

6890 

8320 

9920 

90 

207.9 

115.8 

638 

868 

1136 

1436 

1773 

2140 

2550 

3475 

4530 

5740 

7090 

8560 

10210 

95 

219.4 

119.0 

656 

892 

1168 

1476 

1824 

2200 

2625 

3570 

4655 

5900 

7290 

8800 

10500 

100 

230.9 

122.0 

672 

915 

1196 

1512 

1870 

2255 

2C90 

3660 

4775 

6050 

7470 

9030 

10770 

105 

242.4 

125.0 

689 

937 

1226 

1550 

1916 

2312 

2755 

3750 

4890 

6200 

7650 

9250 

11020 

110 

254.0 

128.0 

705 

960 

1255 

1588 

1961 

23611 

2820 

3840 

5010 

6350 

7840 

9470 

11300 

115 

265.5 

130.9 

720 

980 

1282 

1621 

2005 

2420 

2885 

3930 

5120 

6490 

8010 

9680 

11550 

120 

277.1 

133.7 

736 

1002 

1310 

1659 

2050 

2470 

2945 

4015 

5225 

6630 

8180 

9900 

11800 

125 

288.6 

13G.4 

751 

1022 

1338 

1690 

2090 

2520 

3005 

4090 

5340 

6760 

8350 

10100 

12030 

130 

300.2 

139.1 

767 

1043 

1365 

1726 

2132 

2575 

3070 

4175 

5450 

6900 

8530 

10300 

12290 

135 

311.7 

141.8 

780 

1063 

1390 

1759 

2173 

2620 

3125 

4250 

5550 

7030 

8680 

10490 

12510 

140 

323.3 

144.3 

795 

1082 

1415 

1790 

2212 

2670 

3180 

4330 

5650 

7160 

8850 

10690 

12730 

145 

334.8 

146.9 

809 

1100 

1440 

1820 

2250 

2715 

3235 

4410 

5740 

7280 

8990 

10880 

12960 

150 

346.4 

149.5 

824 

1120 

1466 

1853 

2290 

2760 

3295 

4485 

5850 

7410 

9150 

11070 

13200 

175 

404.1 

161.4 

890 

1210 

1582 

2000 

2473 

2985 

3560 

4840 

6310 

8000 

9890 

11940 

14250 

200 

461.9 

172.6 

950 

1294 

1691 

2140 

2645 

3190 

3800 

5175 

6750 

8550 

10580 

12770 

15220 

250 

577.4 

193.0 

1063 

1447 

1891 

2392 

2955 

3570 

4250 

5795 

7550 

9570 

11820 

14290 

17020 

300 

692.8 

211.2 

1163 

1582 

2070 

2615 

3235 

3900 

4650 

6330 

8260 

1C480 

12940 

15620 

18610 

NOTE — The  actual  quantities  will  vary  from  these  figures,  the  amount  of  varia- 
tion depending  upon  the  shape  of  nozzle  and  size  of  pipe  at  the  point  where  the  pres- 
sure is  determined. 


AND    CONDENSERS    FOR    EVERV  SERVICE 


149 


! 
I 

U  N 

I  0 

N 

STEAM 

P 

UM 

P 

C 

OM 

PANY 

3 

Hydrant  and  Hose  Stream  Data 

From  Tables  Published  by  John  R.  Freeman,  M.E. 


Pressure  at  I 
Nozzle 

.!< 

l|3 
3S  I 

_a>e 

IS! 

II" 

Horizontal 
Distance 
of  Stream 

Pressure  in  pounds  required  at  Hydrant  or  Pump  to  main- 
tain pressure    at    nozzle  through    various  lengths  of  2  H    inch 
smooth,  rubber-lined  hose. 

soft: 

100ft. 

200ft. 

300  ft. 

400  ft. 

500  ft. 

bOO  ft. 

800  ft. 

1000ft. 

INCH  SMOOTH  NOZZLE 


35 

97 

55 

41 

37 

38 

40 

42 

44 

46 

48 

5,) 

57 

40 

104 

60 

44 

42 

43 

46 

48 

50 

53 

55 

60 

65 

45 

110 

64 

47 

47 

48 

51 

54 

57 

59 

62 

68 

73 

50 

116 

67 

50 

52 

54 

57 

60 

63 

66 

69 

75 

81 

55 

122 

70 

52 

58 

59 

63 

66 

69 

73 

76 

83 

89 

60 

127 

72 

54 

63 

65 

68 

72 

76 

79 

83 

90 

97 

65 

132 

74 

56 

68 

70 

74 

78 

82 

86 

90 

98 

106 

70 

137 

76 

58 

73 

75 

80 

84 

88 

92 

97 

105 

114 

75 

142 

78 

60 

79 

81 

85 

90 

94 

99 

104 

113 

122 

80 

147 

79 

62 

84  ' 

86 

91 

96 

101 

106 

111 

120 

130 

85 

151 

80 

64 

89 

92 

97 

102 

107 

112 

117 

128 

138 

90 

156 

81 

65 

94 

97 

102 

108 

113 

119 

124 

135 

146 

95 

160 

82 

66 

99 

102 

108 

114 

120 

125 

131 

143 

154 

100 

164 

83 

68 

105 

108 

114 

120 

126 

132 

138 

150 

16-3 

INCH  SMOOTH  NOZZLE 


35 

133 

56 

46 

38 

40 

44 

48 

52 

56 

60 

68 

76 

40 

142 

62 

49 

43 

46 

50 

55 

59 

64 

68 

78 

87 

45 

150 

67 

52 

49 

51 

57 

62 

67 

72 

77 

87 

97 

50 

159 

71 

55 

54 

57 

63 

69 

74 

80 

86 

97 

108 

55 

166 

74 

58 

60 

63 

69 

75 

82 

88 

94 

107 

119 

60 

174 

77 

61 

65 

69 

75 

82 

89 

96 

103 

116 

130 

65 

181 

79 

64 

71 

74 

82 

89 

96 

104 

111 

126 

141 

70 

188 

81 

66 

76 

80 

88 

96 

104 

112 

120 

136 

152 

75 

194 

83 

68 

82 

86 

94 

103 

111 

120 

128 

145 

162 

80 

201 

85 

70 

87 

91 

101 

110 

119 

128 

137 

155 

173 

85 

207 

87 

72 

92 

97 

107 

116 

126 

136 

145 

165 

184 

90 

213 

88 

74 

98 

103 

113 

123 

134 

144 

154 

174 

195 

95 

219 

89 

75 

103 

109 

119 

130 

141 

152 

163 

184 

206 

100 

224 

90 

76 

109 

114 

126 

137 

148 

160 

171 

194 

216 

1  INCH  SMOOTH  NOZZLE 


35 

174 

58 

51 

40 

44 

51 

57 

64 

71 

78 

92 

105 

40 

186 

64 

55 

46 

50 

58 

66 

73 

81 

89 

105 

120 

45 

198 

69 

58 

52 

56 

65 

74 

83 

91 

100 

118 

135 

50 

208 

73 

61 

57 

62 

72 

82 

92 

102 

111 

131 

151 

55 

218 

76 

64 

63 

69 

79 

90 

101 

112 

122 

144 

166 

60 

228 

79 

67 

69 

75 

87 

98 

110 

122 

134 

157 

181 

65 

237 

82 

70 

75 

81 

.  94 

107 

119 

132 

145 

170 

196 

70 

246 

85 

72 

80 

87 

101 

115 

128 

142 

156 

183 

211 

75 

255 

87 

74 

86 

94 

108 

123 

138 

152 

167 

196 

226 

80 

263 

89 

76 

92 

100 

115 

131 

147 

162 

178 

209 

241 

8b 

274 

91 

78 

98 

106 

123 

1:59 

156 

173 

189 

222 

.  .  . 

90 

279 

92 

80 

103 

112 

130 

147 

165 

183 

200 

236 

95 

287 

94 

82 

109 

118 

137 

156 

174 

193 

211 

249 

100 

295 

96 

83 

115 

125 

144 

164 

183 

203 

223 

The  pressures  given  are  indicated  pressures,  not  effective  pressures. 
Effective  pressures  would  be  slightly  greater. 


ii  Mm«»»«MBji_f  nmjjjj^a  j_^JLJ-1JLM-gJ  "  '  """""•"•"»"  »  »  j  ^gjK^mjgooanra  ffaMM;^  aMr^oca  j  n  n  «  y 

PUMPING    MACHINERY^  AIR__CQMPRES SORS       J 

riT»»auai»uy^Wjni^M^inrTrgTIBttK10U^^ 

150 


Hydrant  and  Hose  Stream  Data 

(Continued] 

From  Tables  Published  by  John  R.  Freeman,  M.  E. 


«a 

OJ 

1 

&a 

3g,6 

Pressure  in  pounds  reQjir^d  at  Hydrant  or   Pump  to  main- 
tain pressure  at    nozzle    through    various    lengths    of    2  H  inch 

I« 

S2  S.S 

^  £?  rt 

sS« 

smooth  rubber-lined  hose. 

g|£ 

•S^  J3 

.85* 

<*>   N 

c  o 

PU»5 

OQ& 

^O'o 

s^^ 

KQ'S 

50ft. 

100ft. 

233ft. 

300  ft. 

400  ft. 

500  ft. 

600  ft. 

800  ft. 

1000  ft. 

\Y%  INCH  SMOOTH  NOZZLE 


35 

222 

59 

54 

43 

49 

60 

71 

82 

94 

105 

127 

149 

40 

238 

65 

59 

50 

56 

69 

81 

94 

07 

120 

145 

171 

45 

252 

70 

63 

56 

63 

77 

92 

106 

120 

135 

163 

192 

50 

266 

75 

66 

62 

70 

86 

102 

118 

134 

150 

181 

213 

55 

279 

80 

69 

68 

77 

95 

112 

130 

147 

165 

200 

235 

60 

291 

83 

72 

74 

84 

103 

122 

141 

160 

180 

218 

256 

65 

303 

86 

75 

81 

91 

112 

132 

153 

174 

195 

236 

70 

314 

88 

77 

87 

98 

120 

143 

165 

187 

209 

254 

75 

325 

90 

79 

93 

105 

129 

153 

177 

201 

224 

80 

336 

92 

81 

99 

112 

138 

163 

188 

214 

239 

. 

85 

346 

94 

83 

106 

119 

146 

173 

200 

227 

254 

90 

356 

96 

85 

112 

126 

155 

183 

212 

241 

1)5 

366 

98 

87 

118 

133 

163 

194 

224 

254 

100 

376 

99 

89 

124 

140 

172 

204 

236 

INCH  SMOOTH  NOZZLE 


35 

277 

60 

59 

48 

57 

74 

91 

109 

126 

142 

178 

212 

40 

296 

67 

63 

55 

65 

84 

104 

124 

144 

164 

203 

243 

45 

314 

72 

67 

62 

73 

95 

117 

140 

162 

184 

229 

50 

331 

77 

70 

68 

81 

106 

130 

155 

180 

204 

254 

55 

347 

81 

73 

75 

89 

116 

143 

170 

198 

225 

60 

363 

85 

76 

82 

97 

127 

156 

186 

216 

245 

65 

377 

88 

79 

89 

105 

137 

169 

201 

234 

. 

70 

392 

91 

81 

96 

113 

148 

182 

217 

252 

75 

405 

93 

83 

103 

121 

158 

195 

232 

80 

419 

95 

85 

110 

129 

169 

208 

148 

85 

432 

97 

88 

116 

137 

179 

221 

'  ' 

90 

444 

99 

90 

123 

145 

190 

234 

95 

456 

100 

92 

130 

154 

201 

247 

100 

468 

101 

93 

137 

162 

211 

261 

INCH  SMOOTH  NOZZLE 


35 
40 
45 
50 
55 
60 

340 
363 

385 
406 

426 
445 

62 
69 
74 
79 

83 

87 

62 
66 
70 
73 
76 
79 

54 
62 
70 
78 
86 
93 

67 
77 
87 
96 
106 
116 

94 
107 
120 
134 
147 
160 

120 
137 
154 
171 

188 
205 

146 
166 
187 
208 
229 
250 

172 
196 
221 
245 
270 

198 
-226 
254 

250 

65 

163 

90 

82 

101 

125 

174 

222 

70 

180 

92 

84 

109 

135 

187 

2;;9 

75 

497 

95 

86 

117 

145 

201 

256 

80 

514 

97 

88 

m 

154 

214 

85 

529 

99 

90 

132 

164 

?,?,7 

90 

545 

100 

9? 

140 

173 

240 

95 

560 

101 

94 

148 

183 

254 

100 

574 

103 

96 

156 

193 

The  pressures  given  are  indicated  pressures,  not  effective  pressures. 
Effective  pressures  would  be  slightly  greater. 


Table  Converting  Inches  Vacuum,  into 
Feet  Suction 


Inch 
Vac. 

Feet 

Inch  Vac. 

Feet 

Inch  Vac. 

Feet 

Inch  Vac. 

Feet 

u 

0.28 

8>4 

9.35 

16J4 

18.42 

24  M 

27.50 

0.56 

8]/o 

9.64 

1^ 

18.71 

y2 

27.78 

si 

0.85 

8% 

9.92 

M 

18.99 

28.07 

l 

1.13 

9 

10.21 

17 

19.28 

25  4 

28.35 

1/4 

1.41 

/4 

10.49 

M 

19.56 

H 

28.63 

1  ^A 

1.70 

y> 

10.77 

19.84 

28.91 

1M 

1.98 

H 

11.06 

M 

20.13 

/4 

29.20 

2 

2.27 

10 

11.34 

18 

20.41 

26 

29.48 

2M 

2.55 

|4 

11.62 

K 

20.70 

/4 

29.76 

2.84 

11.90 

20.98 

1A 

30.05 

2/4 

3.12 

M 

12.19 

/4 

21.27 

H 

30.33 

3 

3.41 

11 

12.47 

19 

21.55 

27 

30.62 

3/4 

3.69 

U 

12.75 

K 

21.83 

/4 

30.90 

3/^ 

3.98 

13.04 

H 

22.11 

i^ 

31.19 

324 

4.26 

% 

13.32 

i 

22.40 

M 

31.47 

4 

4.54 

12 

13.61 

20 

22.68 

28 

31.75 

4/4 

4.82 

/4 

13.89 

/4 

22.96 

^ 

32.03 

4H 

5.11 

VA 

14.18 

Yi 

23.24 

32.32 

4/4 

5.39 

/4 

14.46 

H 

23.53 

M 

32.60 

5 

5.67 

13 

14.74 

21 

23.81 

29 

32.89 

5/4 

5.95 

/4 

15.02 

M 

24.09 

/4 

33.17 

5^2 

6.23 

H 

15.31 

^ 

24.38 

/4 

33.46 

5M 

6.52 

^4 

15.59 

24.66 

M 

33.74 

6 

6.80 

14 

15.88 

22 

24  95 

30 

6M 

7!08 

M 

25!23 

.  .  .  , 

7.37 

i  / 

16^45 

25.51 

60 

7  65 

3/ 

3/ 

25.80 

7  4 

7.94 

15X 

*    17]01 

23 

26.08 

7  1/ 

8.22 

j  / 

17.29 

y. 

26.36 

7*/ 

8.50 

{/ 

X4 

26.65 

10 

8.79 

0 

17  86 

0 

'26  93 

8 

9!07 

16 

18!  14 

24  4 

27.22 

To  convert  inches  vacuum  into  feet,  multiply  by  1.13. 


Relative  Quantities  of  Water 

Delivered  in  24  hours,  in  1  hour  and  in  1  minute. 


Gal's  in 

Gal's  in 

Gal's  in 

Gal's  in 

Gal's  in 

Gal's  in 

Gal's  in 

Gal's  in 

Gal's  in 

24  hours 

1  hour 

1  min. 

24  hours 

1  hour 

1  min. 

24  hours 

1  hour 

1  min 

2500000 

104166.  0 

1736.0 

650000 

27083.3 

451.3 

150000 

6250  0 

104  1 

2000000 

83333.3 

1388.0 

600000 

2;>0l)0  0 

416.7 

100000 

41(>6.6 

69  \ 

1500000 

62500.0 

1041.7 

550000 

22916.6 

381.9 

75000 

3125.0 

52  9 

1000000 

41666.0 

694.3 

500000 

20833.3 

34V.  2 

60000 

2500.0 

41  (i 

950000 

39583.3 

659.7 

450000 

1R'<50.0 

312.5 

50000 

21)83.  0 

34.7 

900000 

37500  0 

625.0 

400000 

16666.  6 

277.7 

25000 

1041.6 

17.3 

850000 

35416.  6 

590.2 

350000 

14583.3 

243.0 

20000 

833.  3 

13.8 

800000 

33333.3 

555.5 

300000 

12500.0 

208.3 

15000 

625.0 

10.4 

750000 

31250.0 

520.8 

250000 

10416.7 

173.6 

10000 

416.6 

6.9 

700000 

29166  6 

486.1 

200000 

8333  0 

138.8 

5000 

208.3 

3  4 

MACHINERY, 
152 


Rules  for  Determining   Size   and  Speed  of 
Pulleys  or  Gears 


The  driving  pulley  is  called  the  Driver,  and  the  driven  pulley 
the  Driven. 

If  the  number  of  teeth  in  gears  are  used  instead  of  diameter, 
in  these  calculations,  number  of  teeth  must  be  substituted  where- 
ever  diameter  occurs. 

To  determine  the  diameter  of  Driver,  the  diameter  of  the 
Driven  and  its  revolutions,  and  also  revolutions  of  Driver  being 
given. 

Diam.  of  Driven  X  revolutions  of  Driven 

— : =Diam.  of  Driver. 

Revolutions  of  Driver. 

To  determine  the  diameter  of  Driven,  the  revolutions  of  the 
Driven  and  diameter  and  revolutions  of  the  Driver  being  given. 

Diam.  of  Driver  X  revolutions  of  Driver 

=Diam.  of  Driven. 

Revolutions  of  Driven. 

To  determine  the  revolutions  of  the  Driver,  the  diameter 
and  revolutions  of  the  driven,  and  diameter  of  the  Driver  being 
given. 

Diam.  of  Driven  X  revolutions  of  [Driven 

! =  Rev.  of  Driver. 

Diameter  of  Driver. 

To  determine  the  revolutions  of  the  Driven,  the  diameter 
and  revolutions  of  the  Driver,  and  diameter  of  the  Driven  being 
given 

Diam.  of  Driver  X  revolutions  of  Driver 

~=Rev.  of  Driven. 
Diameter  ot  Driven. 


153 


Diameter  of  Pulleys  with  Corresponding  Belt 

Speeds  and  Horse  Power  Belting 

will  Transmit 


Diameter  of 
Pulley 
in  Inches 

Belt  Speed  in 
Feet  per  Minute 
per  100  R.  P.  M. 

Corresponding  Horse  Power,  Transmitted 
per  1  in.  Belt  Width 

Single  Belt 

Double  Belt 

3. 

78.6 

.095     • 

.190 

3.82 

100. 

.121 

.242 

4. 

105. 

.127 

.254 

5. 

131. 

.158 

.316 

6. 

157. 

.190 

.380 

8. 

210. 

.254 

.508 

10. 

262. 

.317 

.634 

12. 

314. 

.380 

.760 

14. 

366. 

.443 

.886 

15. 

393. 

.475 

.950 

16. 

419. 

.507 

1.01 

18. 

471. 

.570 

1.14 

20. 

524. 

.634 

1.27 

22. 

576. 

.697 

1.39 

24. 

628. 

.760 

1.52 

26. 

680. 

.823 

1.64 

28. 

733.' 

.888 

1.77 

30. 

785. 

.950 

1.90 

32. 

838. 

1.01 

2.02 

34. 

890. 

1.08 

2.16 

36. 

942. 

1.14 

2.28 

38. 

995. 

1.20 

2.40 

40. 

1048. 

1.26 

2.52 

42. 

1100. 

1.33 

2.66 

48. 

1256. 

1.52 

3.04 

54. 

1415. 

1.71 

3.42 

60. 

1570. 

1.90 

3.80 

66. 

1722. 

2.08 

4.16 

7?. 

1884. 

2.28 

4.56 

R.  P.  M.=Rcvolutions  per  Minute. 

To  find  the  Belt  Speed  in  Feet  per  Minute  for  any  size  pulley  and  any  number  of  revol- 
utions per  minute:  Multiply  the  diameter  of  the  pulley  in  inches  by  the  revolutions  per 
minute,  and  multiply  the  product  by  .262. 

To  find  the  Horse  Power  for  any  width  belt  and  any  speed :  Multiply  the  belt  speed  in 
feet  per  minute  by  the  width  of  the  belt  in  inches,  and  multiply  the  product  by  .00121  for 
a  single  ply  belt,  or  by  .00242  for  a  double  ply  belt.  The  final  result  is  the  horse  power 
which  the  belt  will  transmit. 

EXAMPLE:  What  is  the  speed  of  a  belt  running  over  a  42 
inch  pulley  turning  at  180  R.  P.  M.  ? 

ANSWER:     Belt  speed -42  X  180  X  .262X1980  ft.  per  min. 

EXAMPLE:  What  horse  power  will  a  6  inch  single  ply  belt 
transmit  when  traveling  at  this  speed? 

ANSWER:     Horse  power  =  1980X6 X. 00121  =14.38.. 

Note: — The  horse  power  which  a  belt  will  transmit  as  given  in  the  above  tables  is  based 
on  the  assumption  that  the  pulleys  are  both  of  equal  diameter  or  nearly  so.  When  one 
pulley  is  several  times  larger  than  the  other,  an  extra  allowance  of  width  should  be  made 
to  insure  satisfactory  transmission  of  the  full  amount  of  power.  It  is  always  best  to  have 
a  liberal  sized  belt  for  all  cases,  as  the  liability  of  trouble  of  all  kinds  is  minimized  and  the 
life  of  the  belt  is  greatly  prolonged. 


154 


Theoretical  Horse  Power  Required  to  Raise 
Water  to  Different  Heights 


Feet 
Eleva- 
tion 

5 

10 

15 

20 

25 

30 

35 

40 

45 

50 

60 

Gallons 

per  Min. 

5 

.006 

.012 

.019 

.025 

.031 

.037 

.044 

.05 

.06 

.06 

.07 

10 

.012 

.025 

.037 

.050 

.062 

.075 

.037 

.10 

.11 

.12 

.15 

15 

.019 

.037 

.056 

.075 

.094 

.112 

.131 

"  .15 

.17 

.19 

.22 

20 

.025 

.050 

.075 

.100 

.125 

.150 

.175 

.20 

.22 

.25 

.30 

25 

.031 

.062 

.093 

.125 

.156 

.187 

.219 

.25 

.28 

.31 

.37 

30 

.037 

.075 

.112 

.150 

.187 

.225 

.262 

.30 

.34 

.37 

.45 

35 

.043 

.087 

.131 

.175 

.219 

.262 

.306 

.35 

.39 

.44 

.52 

40 

.050 

.100 

.150 

.200 

.250 

.300 

.350 

.40 

.45 

.50 

.60 

45 

.056 

.112 

.168 

.225 

.281 

.337 

.394 

.45 

.51 

.56 

.67 

50 

.062 

.125 

.187 

.250 

.312 

.375 

.437 

.50 

.56 

.62 

.75 

60 

.075 

.150 

.225 

.300 

.375 

.450 

.525 

.60 

.67 

.75 

.90 

75 

.093 

.187 

.281 

.375 

.469 

.562 

.656 

.75 

.84 

.94 

1.12 

90 

.112 

.225 

.337 

.450 

.562 

.675 

.787 

.90 

1.01 

1.12 

1.35 

100 

.125 

.250 

.375 

.500 

.625 

.750 

.875 

1.00 

1.12 

1.25 

1.50 

125 

.156 

.312 

.469 

.625 

.781 

.937 

1.094 

1.25 

1.41 

1.56 

1.87 

150 

.187 

.375 

.562 

.750 

.937 

1.125 

1.312 

1.50 

1.69 

1.87 

2.25 

175 

.219 

.437 

.656 

.875 

1.093 

1.312 

1.531 

1.75 

1.97 

2.19 

2.62 

200 

.250 

.500 

.750 

1.000 

1.250 

1.500 

1.750 

2.00 

2.25 

2.50 

3.00 

250 

.312 

.625 

.937 

1.250 

1.562 

1.875 

2.187 

2.50 

2.81 

3.12 

3.75 

300 

.375 

.750 

1.125 

1.500 

1.875 

2.250 

2.625 

3.00 

3.37 

3.75 

4.50 

350 

.437 

.875 

1.312 

1.750 

2.187 

2.625 

3.062 

3.50 

3.94 

4.37 

5.25 

400 

.500 

1.000 

1.500 

2.000 

2.500 

3.000 

3.500 

4.00 

4.50 

5.00 

6.00 

500 

.625 

1.250 

1.875 

2.500 

3.125 

3.750 

4.375 

5.00 

5.62 

6.25 

7.50 

Feet 
Eleva- 
tion 

75 

90 

100 

125 

150 

175 

200 

250 

300 

350 

400 

Gallons 

per  Min. 

5 

.09 

.11 

.12 

.16 

.19 

.22 

.25 

.31 

.37 

.44 

.50 

10 

.19 

.22 

.25 

.31 

.37 

.44 

.50 

.62 

.75 

.87 

1.00 

15 

.28 

.34 

.37 

.47 

.56 

.66 

.75 

.94 

1.12 

1.31 

1.50 

20 

.37 

.45 

.50 

.62 

.75 

.87 

1.00 

1.25 

1.50 

1.75 

2.00 

25 

.47 

.56 

.62 

.78 

.94 

1.09 

1.25 

1.56 

1.87 

2.19 

2.50 

30 

.56 

.67 

.75 

.94 

1.12 

1.31 

1.50 

1.87 

2.25 

2.62 

3.00 

35 

.66 

.79 

.87 

1.08 

1.31 

1.53 

1.75 

2.19 

2.62 

3.06 

3.50 

40 

.75 

.90 

1.00 

1.25 

1.50 

1.75 

2.00 

2.50 

3.00 

3.50 

4.00 

45 

.84 

1.01 

1   12 

1.41 

1.69 

1.97 

2.25 

2.81 

3.37 

3.94 

4.50 

50 

.94 

1.12 

1.25 

1.56 

1.87 

2.19 

2.50 

3.12 

3.75 

4.37 

5.00 

60 

1.12 

1.35 

1.50 

1.87 

2.25 

2.62 

3.00 

3.75 

4.50 

5.25 

6.00 

75 

1.40 

1.69 

1.87 

2.34 

2.81 

3.28 

3.75 

4.69 

5.62 

6.56 

7.50 

90 

1.68 

2.02 

2.25 

2.81 

3.37 

3.94 

4.50 

5.62 

6.75 

7.87 

9.00 

100 

1.87 

2.25 

2.50 

3.12 

3.75 

4.37 

5.00 

6.25 

7.50 

8.75 

10.00 

125 

2.34 

2.81 

3.12 

3.91 

4.69 

5.47 

6.25 

7.81 

9.37 

10.94 

12.50 

150 

2.81 

3.37 

3.75 

4.69 

5.62 

6.56 

7.50 

9.37 

11.25 

13.12 

15.00 

175 

3.28 

3.94 

4.37 

5.47 

6.56 

7.66 

8.75 

10.94 

13.12 

15.31 

17.50 

200 

3.75 

4.50 

5.00 

6.25 

7.50 

8.75 

10.00 

12  .  50 

15.00 

17.50 

20.00 

250 

4.69 

5.62 

6.25 

7.81 

9.37 

10.94 

12.50 

15.72 

18.75 

21.87 

25.00 

300 

5.62 

6.75 

7.50 

9.37 

11.25 

13.12 

15.00 

18.75 

22.50 

26.25 

30.00 

350 

6.56 

7.87 

8.75 

10.94 

13.12 

15.31 

17.50 

21.87 

26.25 

30.62 

35.00 

400 

7.50 

9.00 

10.00 

12.50 

15.00 

17.50 

20.00 

25.00 

30.00 

35.00 

40.00 

500 

9.37 

11.25 

12.50 

15.62 

18.75 

21.87 

25.00 

31.25 

37.50 

43.75 

50.00 

The  theoretical  horse  power  required  to  elevate  water  is  found  by 
multiplying  the  gallons  pumped  per  minute  by  the  total  lift  (including 
friction)  in  feet,  and  dividing  by  4000. 


155 


UNION       STEAM       PUMP       COMPANY 


Convenient  Equivalents 

1  second-foot  equals  40  California  miner's  inches.  (Law  of  March 

23,   1901.) 

1  second-foot  equals  38.4  Colorado  miner's  inches. 
1  second-foot  equals  40  Arizona  miner's  inches. 
1  second-foot  equals  7.48    United    States    gallons    per    second; 

equals  448.8  gallons  per  minute ,  equals  646,272  gallons  per  day. 
1  second-foot  equals  6.23  British  imperiargallons  per  second. 
1  second-foot  for  one   year  covers   one  square   mile    1.131   feet 

deep;  13.57  inches  deep. 

1  second-foot  for  one  year  equals  31,536,000  cubic  feet. 
1  second-foot  equals  about  one  acre-inch  per  hour. 
1  second-foot  falling  10  feet  equals  1.136  horsepower. 
100  California  miner's  inches  equal  15.7  United  States  gallons 

per  second. 

100  California  miner's  inches  equal  96.0  Colorado  miner's  inches. 
100  California  miner's  inches  for  one  day  equal  4.96  acre-feet. 
100  Colorado  miner's  inches  equal  2.60  second-feet. 
100  Colorado  miner's  inches  equal   19.5  United  States  gallons 

per  second. 

100  Colorado  miner's  inches  equal  130  California  miner's  inches. 
100  Colorado  miner's  inches  for  one  day  equal  5.17  acre-feet. 
100  United  States  gallons  per  minute  equal  0.223  second  feet. 
100  United  States  gallons  per  minute  for  one  day  equal  0.442 

acre-feet. 

1,000,000  United  States  gallons  per  day  equal  1.55  second-feet. 
1,000,000  United  States  gallons  equal  3.07  acre-feet. 
1,000,000  cubic  feet  equal  22.95  acre-feet. 
1  acre-foot  equals  325,850  gallons. 
1  inch  deep  on  1  square  mile  equals  2,323,200  cubic  feet. 
1  inch  deep  on  1  square  mile  equals  0.0737  second-foot  per  year. 
1  inch  equals  2.54  centimeters. 
1  foot  equals  0.3048  meter. 
1  yard  equals  0.9144  meter. 
1  mile  equals  1.60935  kilometers. 

1  mile  equals  1,760  yards;  equals  5,280  feet;  equals  63,360 inches. 
1  square  yard  equals  0.836  square  meter. 
1  acre  equals  0.4047  hectare. 

1  acre  equals  43,560  square  feet;  equals  4,840  square  yards. 
1  acre  equals  209  feet  square,  nearly. 
1  square  mile  equals  259  hectares. 


AIR   CQMPiyyLSQR-S       J|  1 

v^v^^v-^rirwjnfvwvTinf^^vvvwfTTrrv^rracxaj 


156 


L 

BATTLE 

CREEK. 

MICHIGAN, 

U. 

*    •**••                fl 

1  square  mile  equals  2.59  square  kilometers. 

1  cubic  foot  equals  0.0283  cubic  meter. 

1  cubic  foot  equals  7.48  gallons ;  equals  0.804  bushel. 

1  cubic  foot  of  water  weighs  62.5  pounds. 

1  cubic  yard  equals  0.7646  cubic  meter. 

1  gallon  equals  3.7854  liters. 

1  gallon  equals  8.36  pounds  of  water. 

1  Imperial  Gallon  equals  1.20  U.  S.  Gallons. 

1  gallon  equals  231  cubic  inches  (liquid  measure). 

1  pound  equals  0.4536  kilogram. 

1  avoirdupois  pound  equals  7,000  grains. 

1  troy  pound  equals  5,760  grams. 

1  meter  equals  39.37  inches.         Log.  1.5951654. 

1  meter  equals  3.280833  feet.         Log.  0.5159842. 

1  meter  equals  1.093611  yards.     Log.  0.0388629. 

1  kilometer  equals  3,281  feet;  equals  five-eights  mile,  nearly. 

1  square  meter  equals  10.764  square  feet;  equals  1.196  square 

yards. 

1  hectare,  equals  2.471  acres. 

1  cubic  meter  equals  35.314  cubic  feet;  equals  1.308  cubic  yards. 
1  liter  equals  1.0567  quarts. 
1  gram  equals  15.43  grains. 
1  kilogram  equals  2.2046  pounds. 
1  tonneau  equals  2,204.6  pounds. 
1  foot  per  second  equals  1.097  kilometers  per  hour. 
1  foot  per  second  equals  0.68  mile  per  hour. 
1  cubic  meter  per  minute  equals  0.5886  second-foot. 
Acceleration  of  gravity  equals  32.16  feet  per  second  every  second. 
1  horse  power  equals  550  foot-pounds  per  second. 
1  horse  power  equals  76  kilogram-meters  per  second. 
1  horse  power  equals  746  watts. 
1  horse  power  equals  1  second-foot  falling  8.80  feet. 
1 J  horse  power  equals  about  1  kilowatt. 
To  calculate  water  power  quickly : 

Sec.-feet    X   fall  in  feet 

— — =  Net  horse  power  on  water 

wheel,  realizing  80  per  cent  of  the  theoretical  power. 
1  atm.  equals  14.7   pounds  square  inch  at  sea  level 
1  atm.  equals  33.947  feet  water  at  62°  F. 
1  atm.  equals  30  inches  Mercury  at  62°  F. 
1  atm.  equals  29.92  inches  Mercury  at  32°  F. 


157 


1  atm.  equals  760  mm.  Mercury  at  32°  F. 

1  atm.  equals  1.033  kg.  per  sq.  cm. 

1  Ib.  per  sq.  inch  equals  2.0416  ins.  Mercury  at  62°  F. 

1  Ib.  per  sq.  inch  equals  2.0355  ins.  Mercury  at  32°  F. 

1  Ib.  per  sq.  inch  equals  27.71  ins.  Water  at  62°  F. 

1  Ib.  per  sq.  inch  equals  2.309  feet  of  water  at  62°  F. 

1  Ib.  per  sq.  inch  equals  0.0703  kg.  per  sq.^m. 

1  foot  of  water  at  62°  F.  equals  .433  Ibs.  per  sq.  inch. 

1  inch  of  Mercury  at  62°  F.  equals  .491  Ibs.  per  sq.  inch. 

1  inch  of  Mercury  at  62°  F.  equals  1.132  ft.  of  water  at  62°  F. 


Duty  of  Water  for  Irrigation  in  the  United  States 

The  following  table  is  taken  from  "Irrigation  and  Drainage" 
by  Professor  F.  H.  King  of  the  University  of  Wisconsin : 

Table  showing  the  highest  probable  duty  of  water  per  acre  for 
different  yields  of  different  crops: 


Bushels  Per  Acre.  . 

15 

20 

33 

40 

50 

60 

70 

80 

100 

200 

300 

400 

Name  of  Crop 

Least  Number  of  Acre-Inches  of  Water 

Wheat   
Barley   
Oats 

4.5 
3.21 
2.35 
2.52 

6 
4.28 
3.13 
3.36 
.41 

9 

6.42 
5.70 
5.04 
.62 

12 

8.56 
6.27 
6.72 

.83 

15 

10.7 

7.84 
8.4 
1.03 

18 
12.84 
9.40 
10.08 
1.24 

14.98 

10.98 
11.75 
1.45 

12.54 
13.43 
1.65 

15.68 
16.77 
2.07 

4.U 

"6.2" 

'8.21 

Maize     

Potatoes   

Tons  Per  Acre  

1 

2 

3 

4 

6 

8 

10 

12 

14 

16 

18 

20 

Least  Number  of  Acre-Inches  of  Water 

Clover  Hay 
15  per  cent  water 
Corn  with  ears 
15  per  cent  water 
Corn  silage 
70  per  cent  water 

4.43 

2.08 
1.41  ' 

8.85 
4.16 
2.82 

13.28 
6.24 
4.23 

17.7 
8.32 
5.64 

26.55 
12.47 

8  46 

35.4 
16.61 
11.28 

44.25 
20.72 
14.1 

24.95 
16.92 

29  1 
19.74 

33.26 
22.56 

37.42 

25.38 

41.58 
28  2 

The  above  table  shows  the  minimum  quantity  of  water 
required  to  produce  a  yield  of  40  bushels  of  wheat  per  acre  if 
dependent  entirely  upon  irrigation  to  be  12  inches  in  depth  of 
water  per  acre.  This  is  equal  to  43.560  cubic  feet  or  326.700 
gallons  per  acre.  This  quantity  would  be  distributed  on  the 
land  at  intervals  in  depths  of  from  3  to  4  inches  at  a  time  to 
suit  the  requirements  of  the  growing  crop. 


158 


tjLaaaaaa 


'.I  .5.  .K  ,1  tti  •L.J'US.njJAJJJl.M  A  .a.  AA  S.A-JSJS.  AJSJBJSLJ 


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King  also  gives  the  following 

"It  has  been  shown  that  under  conditions  in  which  no  water 
can  be  lost  by  surface  or  under-drainage : 

Clover  uses  5.089  Acre-inches  in  producing  one  ton  of  dry  matter 
Oats  uses  4.447  Acre-inches  in  producing  one  ton  of  dry  matter 
Barley  uses  4.096  Acre-inches  in  producing  one  ton  of  dry  matter 
Maize  uses  2.391  Acre-inches  in  producing  one  ton  of  dry  matter 
Potatoes  use  3.399  Acre-inches  in  producing  one  ton  of  dry  matter 

"These  figures  are  an  approximate  measure  of  the  demands 
of  those  crops  for  water  and  if  one,  two  or  three  tons  of  dry 
matter  per  acre  are  to  be  produced  by  these  crops,  then  the 
amount  of  available  rainfall  needed  will  be  given  by  multiplying 
the  figures  in  this  table  by  the  yield  which  is  expected  per  acre 
from  the  soil." 

Open  Ditches 

A  drainage  ditch  should  be  of  sufficient  capacity  to  flow 
only  three-fourths  full  at  flood  height. 

A  channel  with  vertical  sides  offers  least  resistance  to  cur- 
rent, and  if  this  form  could  be  maintained,. it  would  carry  greatest 
volume  of  water  in  proportion  to  its  cross  section  area.  But 
since  nothing  but  rocky  material  will  stand  in  this  form,  most 
ditches  are  made  trapezoidal  in  cross  section.  Ordinary  clays 
will  stand  with  a  slope  of  45°  or  1  to  1.  Loose  loamy  and  sandy 
soils  usually  require  slopes  of  \l/2  to  1. 

Ditches  should  have  sufficient  fall  to  make  them  self-clean- 
ing. In  soil  and  clay  not  easily  displaced,  this  is  about  4  feet 
per  mile,  which  for  ditches  of  ordinary  size  gives  a  mean  velocity 
of  2^4  miles  per  hour  when  running  full.  Increasing  the  depth 
of  a  ditch  increases  the  head  so  that  ditches  of  light  grade  chan- 
nels should  be  made  as  deep  as  possible. 

The  greatest  velocity  of  a  stream  is  found  in  the  thread  of 
current  in  the  center  of  the  channel  just  below  the  surface. 
All  other  parts  have  a  less  velocity  in  proportion  as  they  approach 
the  bottom  and  sides  of  the  channel.  The  mean  velocity  in  a 
trapezoidal  ditch  is  about  four-fifths  of  the  surface  velocity  and 
is  that  found  at  a  point  in  the  center  line  of  the  ditch  a  little 
more  than  half  way  from  the  surface  to  the  bottom.  The  bot- 
tom velocity  is  about  seven -tenths  that  of  the  surface. 

The  following  table  taken  from  "Engineering  for  Land 
Drainage",  by  Charles  G.  Elliott,  shows  the  effect  that  increase 
in  depth  has  upon  the  mean  velocity  in  a  rectangular  channel 
10  feet  wide  with  a  grade  of  3  feet  per  mile. 


jj       AND   CONDENSERS 

FOR   EVERY  SERVICE 

1 

159 


UNION       STEAM       PUMP 


Mean  Velocity  of  Water  at  Different  Depths  in 

Rectangular  Ditch  10  Feet  Wide, 

Grade  3  Feet  per  Mile 

Mean  Velocity 
Depth  in  Feet  in  Feet  per  Second 

0.5  1.4 

1.5  2.3 

2.0  2.6 

2.5  2.3 

3.0  2.9 

4.0  3.2 

5.0  3.4 

6.0  3.6 

8.0  3.8 

Relation  of  Breadth  and  Depth  of  Channel 
to  Surface  and  Mean  Velocity 

The  following  table  from' Tanning's  Hydraulic  Engineering, 
shows  the  relation  of  breadth,  depth,  surface  velocity  and  mean 
velocity  to  each  other  for  rectangular  smooth  channels  when 
water  is  from  5  to  10  feet  deep.     Let  b  = breadth,  d  =  depth,  V 
^surface  velocity  and  v=mean  velocity. 

When  b  =  2d  then  v  =  .920V 

When  b  =   3d  then  v  =  .910V 

When  b  =  4d  then  v  =  .896V 

When  b  =  5d  then  v  =  .882V 

When  b  =   6d  then  v  =  .864V 

Whenb  =  7d  then  v  =  .  847V 

When  b  =  8d  then  v  =  .826V 

When  b  =  9d  then  v  =  .805V 

When  b=10d  then  v  =  .780V 

The  mean  velocity  for  a  trapezoidal  channel  will  be  a  little 
less  and  decreases  as  the  sides  slopes  are  flattened. 

Safe  Velocity  of  Flow  in  Ditches 

The  safe  velocity  is  the  highest  velocity  at  which  it  is  safe 
to  allow  water  to  flow  in  a  ditch  to  prevent  erosion  or  washing 
of  banks.  Ditches  should  be  made  as  nearly  self  cleaning 
as  possible  and  this  often  requires  increasing  the  velocity  of 
flow,  particularly  where  water  carries  a  large  amount  of  silt, 
to  practically  the  limit  of  safety. 

Kents  Eng.   Hand  Book  gives  the  following: 


I 


PUMPING   MACHINE ^ 

160 


L 

BATTLE 

C 

RE 

EK. 

MIC 

HIG 

AN, 

U. 

s. 

A. 

1 

Safe  Velocity  of  Water  in  Ditches  in  Feet 
Per  Minute 

Soft  Brown  Earth 18  ft. 

Soft  Loam 36  ft. 

Pure  Sand -~~  66  ft. 

Gravel - 156  ft. 

Sandy  Soil  15%  clay .- 72  ft. 

Sandy  Soil  40%  clay 108  ft. 

Loamy  Soil  65%  clay 180  ft. 

Clay  Loam  85%  clay 288  ft. 

Agricultural  Clay  95%  clay 372  ft. 

Clay......... 432  ft. 

The  quantity  of  water  any  ditch  will  convey  safely  depends 
on  the  gradient,  the  kind  of  soil,  the  depth  of  ditch,  and  whether 
cut  to  templet  from  solid  earth  or  cut  irregularly  and  banks 
allowed  to  cave  and  form  a  deflection  of  the  stream  from  side  to 
bide. 

Irrigation  Quantity  Tables 


Gallons  required 

Amount  of  Water  Required 
to  Cover  One  Acre  to 

Second  Feet  Reduced  to  Gallons 

to  cover  a    given 
number  of    acres 

Given  Depths 

and  Acre  Feet 

to  a  depth  of  one 

foot.   (Acre  foot) 

«           0 

*  e  8.S 

1  SI 

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3630 

27154 

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112.2 

80790 

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325851 

2" 

7260 

54309 

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224.4 

161579 

.4959 

2 

651703 

3" 

10890 

81463 

3^ 

336.6 

242369 

.7438 

3 

977554 

4" 

14520 

108617 

1 

448.8 

323158 

.9917 

4 

1303406 

5" 

18150 

135771 

1/4 

561.0 

403948 

1.2397 

5 

1629257 

6" 

21780 

162926 

1  /^ 

673.2 

484738 

1.4876 

6 

1955109 

7" 

25410 

190080 

1M 

785.5 

565527 

1.7355 

7 

2280960 

8" 

29040 

217234 

2    • 

897.7 

646317 

1.9835 

8 

2606812 

9" 

32670 

244389 

23^ 

1122.1 

807896 

2.4793 

9 

2932663 

10" 

36300 

271542 

3 

1346.5 

969475 

2.9752 

10 

3258515 

11" 

39930 

298697 

4 

1795.3 

1292634 

3.9669 

15 

4887772 

1'    00" 

43560 

325851 

5 

2244.2 

1615792 

4.9586 

20 

6512029 

1'      2" 

50820 

380160 

6 

2693.0 

1938951 

5.9503 

25 

8146285 

1'      4" 

58080 

434469 

7 

3141.8 

2262109 

6.9421 

30 

9775544 

1'      6" 

65340 

488777 

8 

3590.6 

2585268 

7.9338 

40 

13034058 

1'      8" 

72600 

543086 

9 

4039.5 

2908426 

8.9255 

60 

19551087 

I7    10" 

79860 

597394 

10 

4488.3 

3231585 

9.9173 

80 

26068116 

2'    00" 

87120 

651703 

20 

8976.6 

6463170 

19.8345 

160 

52136232 

One  cubic  foot  of  water  per  second  (exact  7.48052  gallons),  constant 
flow  is  known  as  the  "Second  Foot".  The  "Acre  Foot"  is  the  quantity 
of  water  required  to  cover  one  acre  to  a  depth  of  one  foot. 


161 


STEAM       PUMP       COMPANY 


es  and  Canals 


of  Standard  Irrigation 


Capaci 


ation  ditches  with  low  gradient 
pending  upon  soil  conditions  and 


g 


-half  to  one  and  is  adapted  only  for 
with  slopes  of  from  1  to  1,  to  l}4  to. 


able  gives  a  slope  of  bank 
Drainage  ditches  require 


The  following 
a  sluggish  flo 
it 


-9.1  9q 


0  Feet  Pe 
Mile 


oj 

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93-lBlSl 


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1  Foot 
Per  Mile 


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JO   B9JV 


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be  r 
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n  have 
surfac 
permit 
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porati 
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oil  wi 
d  fro 
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he  surfac 
and  eva 
ct  propo 
as  the  s 
as  revise 
Agricult 


puting  the  volume 
hes  follow  th 
rom  seepage 
s  are  in  dire 
in  the  ditch 
This  table  w 
partment  of 


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the  dit 
Losses 
source 
f 
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the 
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162 


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ATT 

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EK. 

MIC 

HIG 

AN, 

U. 

S. 

A. 

J 

Velocity  of  Flow  of  Water  in  Feet  per  Second 
Through  Various  Sized  Pipes 


U.   S.   GALLONS   PER  MINUTE 


100 

150 

200 

250 

300 

350 

400 

450 

500 

600 

700 

^800 

900 

1000 

4.539 
2.553 
1.634 
1.135 
.834 
.638 
.504 

6.808 
3.829 
2.451 
1.702 
1.250 
.957 
.756 
.613 

9.078 
5.106 
3.268 
2.269 
1.667 
1.277 
1.009 
.817 
.675 

11.347 

6.382 
4.085 
2.837 
2.084 
1.596 
1.261 
1.021 
.844 
.709 
.604 
.521 

13.616 
7.660 
4.902 
3.404 
2.501 
1.914 
1.513 
1.226 
1.013 
.851 
.725 
.625 
.545 

8.936 
5.  719 
3.971 
2.917 
2.233 
1.765 
1.430 
1.182 
.993 
.846 
.729 
.635 
.558 

10.212 
6.  536 
4.538 
3.335 
2.553 
2.017 
1.634 
1.350 
1.135 
.967 
.834 
.726 
.638 
.504 

11.488 
7.353 
5.105 
3.752 
2.872 
2.269 
1.838 
1.519 
1.277 
1.088 
.938 
.817 
.718 
.567 

12.765 
8.170 
5.673 
4.168 
3.191 
2.521 
2.043 
1.688 
1.418 
1.209 
1.042 
.908 
.798 
.630 
.511 

9.804 
6.808 
5.002 
3.829 
3.026 
2.451 
2.026 
1.702 
1.450 
1.251 
1.089 
957 
.756 
.613 

11.438 
7  943 
5.836 
4.467 
3.530 
2.860 
2.364 
1.986 
1.692 
1.459 
1.271 
1.117 
.882 
715 
.496 

13.072 
9.078 
6.669 
5.105 
4.035 
3.268 
2.700 
2.269 
1.934 
1.667 
1.452 
1  276 
1.009 
.817 
.567 

10.212 
7.503 
5.744 
4.539 
3.676 
3.039 
2.553 
2.176 
1.876 
1.634 
1.436 
1.135 
.919 
.638 

11.347 
8.336 
6.382 
5.043 
4.085 
3.376 
2.837 
2.417 
2.085 
1.816 
1.596 
1.261 
1.021 
.709 
.454 

.567 

Velocity  of  Flow  of  Water  in  Feet  per  Second 
Through  Various  Sized  Pipes 


U.   S.   GALLONS   PER  MINUTE 


E  = 

11 

1250 

1500 

1750 

2000 

2500 

3000 

4000 

5000 

7500 

10000 

15000 

20000 

25000 

6 

14.184 

7 

10.421 

12.505 

14.589 

16.673 

8 

7.978 

9.571 

11.168 

12.765 

9 

6.304 

7.566 

8.827 

10.087 

12.609 

15.130 

10 

5.106 

6.127 

7.149 

8.170 

10.213 

12.255 

16.  340 

11 

4.220 

5.064 

5.908 

6.752 

8.440 

10.128 

13.  504  116.  880 

12 

3.546 

4.255 

4.964 

5.673 

7.091 

8.510 

11.34614.183 

13 

3.022 

3.625 

4.2301  4.834 

6.043 

7.252 

9.669 

12.086 

18.129 

14 

2.606 

3.127 

3.648J  4.169 

5.211 

6.254 

8.338 

10.421 

15.632 

15 

2.268 

2.724 

3.177!  3.631 

4.539 

5.447 

7.262 

9.078 

13.616 

18.155 

16 

1.995 

2.394 

2.793i  3.181 

3.989 

4.787 

6.382 

7  978 

11  967 

15.956 

18 

1.576 

1.891 

2.206!  2.521 

3.152 

3.782 

5.043 

6.303 

9  455 

12.607 

18.912 

20 

1.277 

1.532 

1.787 

2.043 

2.553 

3.064 

4.085 

5.106 

,  659 

10.213 

15.319 

24 

.887 

1.064 

1.241 

1.418 

1.773 

2.128 

2.837 

3.546 

8.319 

7.092 

10.638 

14.184 

30 

.567 

.681 

.794 

.908 

1.135 

1.362 

1.816 

2.269 

3.404 

4.539 

6.809 

9.078 

11.347 

36 

473 

630 

.788 

.946 

1  261 

1  576 

2.364 

3.152 

4.728 

6  304 

7  880 

42 

.463 

.579 

.695 

.926 

1.158 

1  737 

2  316 

3  474 

4  631 

5  789 

48 

.443 

.532 

.709 

.886 

1.329 

1.773 

2.659 

3!  546 

4.433 

r 


UNION       STEAM       PUMP 


«f """""' T-"""*        

COMPANY 


Flow  of  Water  in  Flumes 


Velocity  in  feet  per  second,  and  quantity  in  gallons  per  minute 
For  various  sizes  and  slo'pes. 


If 

1 

ij 

°"S 

iJ 

cct 

^ 

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0 

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Velocity 
G.P.M. 

1.2 
270 

1.6 
825 

1.9 
1725 

2.6 
5200 

3.2 
11475 

3.7 

20850 

4.2 

33750 

4.6 

50250 

5.0 
72000 

5.4 

97500 

5.8 
130500 

»-i  "c 

c 

Velocity 
G.  P.  M. 

1.7 

382 

2.2 

1130 

2.7 

2430 

3.7 

7500 

4.5 
16200 

5.2 

29250 

5.9 

47625 

6.5 
71520 

7.1 

102000 

7.7 
140250 

21 

Eg 

— 

S 

.s 

Velocity 
G.P.M. 

2.4 
540 

3.1 

1560 

3.9 
3510 

5.2 

10500 

6.4 
22950 

7.4 
41G25 

II 

c 

Velocity 
G.  P.  M. 

2.3 
650 

3.8 
1920 

4.8 
4312 

6.4 
12900 

7.8 
28050 

Velocity 

3.3 

4.4 

5.5 

7.3 

G.  P.  M. 

742 

2220 

4950 

14775 

.S 

Velocity 
G.  P.  M. 

1.7 
382 

2.3 
1162 

2.7 
2430 

3.6 
7275 

4.4 
15750 

5.0 
28125 

5.6 

45000 

6.2 

68250 

6.8 

97500 

7.3 
187500 

7.7 
172500 

s 

6 

.S 

.    Velocity 

2.4 

3.2 

3.9 

5.1 

6.2 

7.1 

8.0 

-H4 

^ 

G.  P.  M. 

540 

1620 

3510 

10275 

22350 

39750 

64500 

s« 

2 

go 

M? 

s 

Velocity 

3.4 

4.5 

5.5 

7  2 

0  rt 
to    . 

CO 

G.  P.  M. 

765 

2250 

4950 

1455' 

is 

c 

Velocity 

4.1 

5.5 

6.7 

•^TJ 

^ 

G.P.M. 

915 

2775 

6037 

B 

•* 

S 

c 

Velocity 

4.8 

6.4 

7.7 

<o 

G.P.M. 

1072 

3225 

6937 

164 


S£ 


Condensers 


H       SECTION  THREE 

^  Cl 


& 


Condensers 

Condensers  are  used  in  connection  with  steam  engines  and 
steam  turbines  for  the  purpose  of  obtaining  one  of  two  important 
results,  and  generally  both  of  them,  viz. ;  a  reduction  in  the  con- 
sumption of  steam,  and  the  obtaining  of  more  power  from  a 
given  weight  of  steam. 

To  illustrate  the  action  of  a  condenser,  consider  a  simple 
idle  steam  engine.  The  atmosphere  exerts  a  pressure  of  14.7 
pounds  per  square  inch  on  both  sides  of  the  steam  piston,  and 
since  the  pressures  are  equal,  they  balance  each  other,  and  the' 
piston  cannot  move.  If  the  pressure  of  the  atmosphere  on  one 
side  of  the  piston  is  partially  removed,  the  pressure  on  the 
opposite  side  will  then  be  the  greater,  and  the  piston  will  move. 
Thus  it  will  be  seen  that  by  removing  the  atmospheric  pressure 
from  one  side  of  the  piston,  sufficient  pressure  may  be  obtained 
to  move  the  piston  without  taking  any  steam  from  the  boiler. 

It  is  the  office  and  duty  of  the  condenser  to  remove  a  part  of 
the  atmospheric  pressure  from  one  side  of  the  piston,  thus  en- 
abling the  higher  atmospheric  pressure  on  the  other  side  to  move 
the  piston.  If  the  engine  will  then  run  fast  enough  to  develop, 
say  ten  per  cent  of  its  rated  power,  then  the  condenser  will 
add  ten  per  cent  to  the  power  of  the  engine,  because  thus  far 
no  steam  has  been  taken  from  the  boiler — we  have  simply  re- 
moved a  part  of  the  atmospheric  pressure  or  resistance  to  the 
piston. 

When  the  atmospheric  pressure  is  partially  removed  from 
one  end  of  the  cylinder,  as  soon  as  the  piston  reaches  the  end  of 
the  stroke,  the  higher  pressure  on  the  opposite  side  will  act,  and 
this  will  continue  as  long  as  the  exhaust  valve  remains  open,  or 
through  practically  the  whole  stroke;  it  is  the  average  pressure 
for  the  stroke,  and  consequently  the  difference  between  the  high 
pressure  on  one  side,  and  the  low  pressure  on  the  other  side, 
representing  the  mean  effective  pressure.  This  is  the  M.  E.  P. 
due  to  the  condenser,  and  it  will  remain  the  same  regardless  of 
the  steam  pressure. 

Now  when  we  know  the  M.  E.  P.  produced  by  the  condenser, 
it  is  possible  to  find  the  horse  power  due  to  the  condenser.  Know- 
ing the  M.  E.  P.  due  to  the  condenser,  and  the  M.  E.  P.  pro- 
duced by  the  steam,  it  is  possible  to  find  the  horse  power  of  the 
engine,  when  operating,  non-condensing  and  condensing. 


166 


|       BATTLE 

C 

RE 

E 

K, 

M 

1C 

H 

IGAN, 

U. 

S.  A. 

When  the  pressure  in  any  engine  is  less  than  14.7  Ibs.  per 
square  inch  (at  sea  level),  a  partial  vacuum  is  said  to  exist. 
Thus  when  a  condenser  removes  a  part  of  the  atmospheric  pres- 
sure from  one  side  of  the  piston,  a  partial  vacuum  will  exist.  A 
condenser  (with  its  auxiliaries)  produces  a  vacuum  in  two  ways: 
first,  by  removing  the  air  from  the  condensing  chamber,  exhaust 
pipe  and  cylinder;  and  second,  by  condensing  the  steam,  which 
flows  into  it,  thus  causing  it  to  return  to  a  liquid — water. 

If  a  cubic  inch  of  water  is  evaporated  at  atmospheric  pres- 
sure (14.7  Ibs.  absolute)  or  no  pressure  (by  gauge),  it  will  occupy 
1642  cubic  inches,  and  will  displace  1642  cubic  inches  of  air. 
If  the  steam  thus  produced  be  confined  in  an  air  tight  receptacle, 
and  condensed,  it  will  return  to  water,  and  will  then  occupy  nrV* 
of  the  space  formally  occupied.  Since  no  air  can  enter  the  recep- 
tacle, a  vacuum  will  be  produced.  Thus  if  the  exhaust  pipe, 
cylinder,  or  condensing  chamber  be  filled  with  steam,  the  air 
driven  out,  and  if  these  parts  are  air  tight  and  the  steam  be  con- 
densed, a  vacuum  will  exist  in  the  condenser,  the  exhaust  pipe, 
and  cylinder.  The  vacuum  in  a  condensing  engine  is,  therefore, 
produced  by  condensing  the  steam,  and  by  removing  the  small 
amount  of  air  that  enters  with  the  steam,  together  with  what 
leaks  in. 

For  non-condensing  engines  where  the  steam  exhaust  is 
direct  to  the  atmosphere,  at  least  the  pressure  of  the  atmosphere 
must  act  against  the  exhaust  side  of  the  piston,  but  in  practice 
the  back  pressure  is  seldom  less  than  17  or  18  Ibs.  absolute, 
whereas,  the  back  pressure  acting  against  the  exhaust  side  of 
the  piston  of  a  good  condensing  engine  is  often  as  low  as  2  l?^s. 
absolute. 

Assume  an  engine  is  running  without  a  condenser  at  a  mean 
effective  pressure  of  say  60  Ibs.  per  square  inch,  and  a  condenser 
is  added  removing  say  14  Ibs.  of  back  pressure ;  the  mean  effective 
pressure  would  be  increased  theoretically  to  74  Ibs.,  and  the 
power  of  the  engine  would  be  correspondingly  increased. 

If  the  work  done  by  the  engine,  after  installing  the  con- 
denser, remains  the  same,  the  mean  effective  pressure  may  be 
reduced  again  to  60  Ibs.  by  cutting  off  the  steam  earlier  in  the 
stroke,  and  thus  effecting  a  saving  in  steam  consumption. 
Therefore,  if  the  mean  effective  pressure  produced  by  the  con- 
denser is  known,  one  may  readily  estimate  the  horse  power 
added  by  the  condenser. 

If  it  is  desired  to  find  the  horse  power  added  by  the  conuenser, 
the  following  formula  may  be  employed: 


AXRXS 

-"  (35) 


Where  G  =  Gain  in  horse  power  due  to  the  condenser, 

A— Area  of  piston  in  square  inches. 

R  —Reduction  in  back  pressure  in  Ibs.  per  square  inch 

S=  Piston  speed  in  feet  per  minute. 

The  reduction  in  back  pressure  R  on  the  engine  piston  may 
be  estimated  as  follows: 

(36) 

Where  B  =  Absolute  back  pressure  in  pounds  per  square 
inch  on  the  engine  piston  when  running  non-condensing,  V  = 
vacuum  in  inches  of  mercury  (referred  to  a  30  *  barometer) 
produced  by  the  condenser. 

Generally  speaking,  a  n  on -con  den  sing  engine  requires  from 
20  to  30%  more  steam  per  horse  power-hour,  than  a  condensing 
engine  of  the  same  power.  If  a  condenser  be  added  to  a  non- 
condensing  engine  of  say  250  H.  P.  running  at  100  revolutions 
per  minute,  and  the  load  and  speed  be  kept  the  same  after  adding 
the  condenser,  the  governor  will  produce  an  earlier  cut-off, 
thus  lowering  the  mean  forward  pressure  of  the  steam,  and 
the  mean  effective  pressure  will  remain  constant. 

Suppose  the  cut-off  occured  at  X  stroke  when  running  non- 
condensing,  and  at  K  stroke  when  running  condensing,  neglect- 
ing clearance,  the  saving  in  steam  per  stroke  is  the  difference 
between  >£  and  }4,  the  piston  displacement,  or 


.5 

Neglecting  friction  and  other  losses,  the  theoretical  mean 
effective  pressure  may  be  determined  as  follows : 

(1+HYP.  logr) 
M.  E.  P.-PX-       -^~  —  P  (37) 

Where 

P=  Absolute  initial  pressure  in  Ibs.  per  square  inch. 
p  =  Absolute  back  pressure  in  Ibs.  per  square  inch. 
r=  Ratio  of  expansion  = 

Length  of  stroke  +  Clearance 

Distance  to  cut  off  +  Clearance 

The  following  table  shows  the  mean  pressure  per  pound  of 
initial  pressure  with  different  clearance  and  cut-offs. 


f 

n 


168 


oooooooooooooooo 


OOOOOOOOOOOO..OOOO 


oooooooooooooooo 


oooooooooooooooo 


O  O  O  O  O  O  O  O  O  O  O  o  O  o  O  O 


oooooooooooooooo 


o  o  o  o  o  o  o  o  o"  o  o  o  o  o'  o  o' 


ooooooooooo.  ooooo 


ooooooooooo  o  o  ooo 

CO    CO    O5    i-H    r- (C^C^OSi— I    CO    »-H    Oi    i— t    00    i— I    CO 

oooooooo  o  o'  o  o'  o  o*  o'  o 


o  o  o  o  o  o  o  ooo 


o  o  o  o  o  o  o  o 


o  o  o  o  o  o 


ooo  o 


*.;    •;_.     Ti;     —  <«'J    **•>  uj    !>» 

222Si2OCY:)l>-ooo(Noo 

...""" '^C^OOCOCOTjHiOOcDOt^- 

o  o  o  o'  o'  o  Q'  o  o  o  o  o'  o  o  o 


Assuming  a  single  non  -condensing  engine  having  a  clearance 
of  5  per  cent,  and  cutting  off  at  Y\  stroke.  Let  the  steam 
pressure  at  the  throttle  be  150  Ibs.  absolute  and  the  back  pressure 
17  Ibs.  absolute.  It  is  also  assumed  that  the  initial  pressure  in 
the  cylinder  is  the  same  as  the  pressure  at  the  throttle. 

Referring  to  the  column  headed  "5  per  cent  clearance," 
opposite  ^  cut  off,  the  mean  pressure  per  pound  of  initial  pres- 
sure will  be  found  to  be  equal  to  .  6258.  This  multiplied  by  the 
initial  pressure  is 

150  X.  6258  =93.87  Ibs. 

which  is  the  mean  forward  pressure  of  the  steam.     Subtracting 
the  absolute  back  pressure, 

93.87—17-76.87  Ibs.  per  square  inch 
as  the  mean  effective  pressure  on  the  piston. 

Let  it  be  required  to  find  an  approximate  point  of  cut-off, 
which  will  maintain  the  same  power  of  the  engine,  when  running 
condensing  with  a  vacuum  of  26  ",  and  it  be  understood  that  the 
speed  and  load,  and  consequently  the  initial  and  mean  effective 
pressure  remain  the  same. 

Dividing  26  "  of  vacuum  by  2.04  (1  pound  pressure  =2.04 
inches  of  mercury),  gives  12.7  pounds  per  square  inch,  and  sub- 
tracting this  from  the  atmospheric  pressure,  leaves  2  pounds  as 
the  approximate  absolute  back  pressure  on  the  piston.  Ihe 
mean  pressure  ratio  for  the  foregoing  conditions  may  be  found  by 
adding  the  mean  effective  pressure  to  the  absolute  back  pressure, 
and  dividing  by  the  absolute  initial  steam  pressure. 

Substituting  the  actual  values: 


150 

as  the  mean  pressure  ratio  required. 

Referring  again  to  the  table  and  following  down  the  column 
headed  "5%  Clearance",  .5258  will  be  found  to  be  between  the 
values  .5096  and  .5405.  Taking  .5405  as  the  nearest  figure  in 
the  table,  it  is  found  to  correspond  to  a  cut-off  of  A  or  18.8 
per  cent  of  the  stroke. 

The  approximate  saving  in  steam  is  : 

OK  _  1  CQ 

-X  100=  24.8  per  cent. 
.25 

due  to  adding  the  condenser,  and  thereby  shortening  the  cut-off. 
If  the  saving  in  fuel  is  assumed  to  be  in  direct  proportion 


M««»m.miHiiii»i.«<ii.«Ma^n»Hi»uaMaffi»Jn»fflati  JLJ*AM*^  JJ^JULJUCSKX:/*  a.  <a  a  /MLP«^  ^gS&^SJyi^g^Eg 

PUMPING    MACHINERY,    AIR   COMPRESSORS         H 

nrjrgTTWTrgwww^a^r^^lTMir^ 


170 


to  the  saving  in  steam,  the  condensing  engine  in  this  case  will 
require  24.8  per  cent  less  fuel,  than  the  same  engine  would  run 
ning  non -condensing. 

The  increase  in  economy  by  the  use  of  a  condenser  with  a 
steam  engine  may  be  shown  graphically  as  follows : 


Fig.  74. 


Let  ABCDEF,  figure  74,  be  the  indicator  card  from  a  non- 
condensing  engine.  M-N  is  the  atmospheric  line,  and  O-X  is 
the  vacuum  line.  The  back  pressure  as  shown  by  the  card, 
is  O-S.  The  area  of  the  card  represents  to  some  scale  the  work 
done  per  stroke.  Now  let  a  condenser  be  attached  to  the  en- 
gine, and  the  back  pressure  will  be  lowered  to  O-T,  the  line  H-K, 
instead  of  D-E  now  being  the  lower  line  of  the  card,  and  ABCHKL 
will  be  the  new  card,  and  its  area  as  before,  represents  the  work 
done  per  stroke.  Hence  by  adding  a  con  denser  "to  the  engine, 
the  work  done  per  stroke  has  been  increased  by  an  amount 
represented  by  the  area  FEDHKL,  the  steam  consumption  re- 
maining the  same. 

Suppose  the  steam  be  cut  off  at  a  point  P,  making  the  area 
of  the  card  APGHKL  equal  to  the  area  of  the  original  card 
ABCDEF;  then  the  work  per  stroke  is  the  same  in  both  engines, 
but  the  condensing  engine  uses  an  amount  of  steam  per  stroke 
represented  by  the  length  A-P,  while  the  non -condensing  engine 
uses  an  amount  of  steam  represented  by  A-B.  Either  case  shows 
the  economy  of  the  condenser. 


1"^  AND 

kr™™rw™rw. 

CONDENSERS 

FOR 

EVERY 

SERVICE         | 

171 


Gain  in  Thermal  Efficiency 

The  gain  in  thermal  efficiency  due  to  adding  a  condenser 
to  a  steam  engine  or  turbine,  may  be  calculated  as  follows  : 

Let 

E  =  Thermal  efficiency  of  engine  or  turbine. 

T!  =  Absolute  temperature  at  which  the  steam  is  received  by 
the  engine. 

T2=The  absolute  temperature  at  which  the  steam  is  ex- 
hausted from  the  engine  or  turbine. 

Then  for  a  perfect  engine 

T         T 

E=-2  (38) 


The  efficiency  of  an  engine  or  turbine  may  be  increased 
by  raising  the  boiler  pressure,  and  thus  increasing  Tlf  or  by  reduc- 
ing the  back  pressure  by  adding  a  condenser,  thus  decreasing  T2, 
or  by  doing  both.  It  is  evident  from  the  formula  that  by  re- 
ducing the  back  pressure,  a  much  greater  gain  in  efficiency  re- 
sults than  by  raising  the  boiler  pressure  a  like  amount.  This  is 
shown  in  the  following  examples. 

Suppose  a  non-condensing  engine  or  turbine  is  supplied 
with  steam  at  150  pounds  absolute,  as  in  the  previous  example, 
and  exhausts  at  17  pounds  absolute,  the  absolute  temperature 
Tx  corresponding  to  150  pounds  is  (by  referring  to  Steam  Table 
in  appendix)  : 

358.5  +  461  =819.5  degrees  Fah. 

The  absolute  temperature  T2,  corresponding  to  17  pounds 
absolute  pressure,  is: 

219.4  +  461=680.4  degrees  Fah. 

Hence  the  thermal  efficiency  is: 

819.5—680.4 
~- 


Or  17  per  cent. 

Now  suppose  the  boiler  pressure  be  raised  from  150  pounds 
absolute  to  200  pounds  absolute,  and  the  exhaust  pressure  kept 
the  same,  then  the  absolute  temperature  T1  corresponding  to 
200  pounds  absolute  is  842.9  degrees  Fahrenheit,  and  the  abso- 
lute temperature  T2  corresponding  to  17  pounds  absolute  is 
680.4  degrees  Fahrenheit.  Hence  the  thermal  efficiency  is: 

842.9—  680.4  _ 

T-  ~"~  "        ~  ••     -  -  .  J.  *7O 

842.9 
or  19.3  per  cent. 


172 


pr 

A 

TTLI 

.       C  I 

l.EE 

K. 

M 

1C  H 

IG 

AN. 

U.  S.  A. 

1 

Suppose  instead  of  raising  the  boiler  pressure,  the  steam 
engine  or  turbine  be  connected  up  to  a  condenser,  thus  reducing 
the  back  pressure  from  17  pounds  to  2  pounds  absolute.  The 
absolute  temperature  T2  corresponding  to  2  pounds  absolute 
is  587.15  degrees  Fahrenheit,  and  the  absolute  temperature  T3, 
as  already  found,  was  819.5  degrees  Fahrenheit.  In  this  case 
the  thermal  efficiency  would  be: 

819.5-587.15 
819.5 

or  28.3  per  cent. 

From  the  foregoing,  it  is  evident  that  by  lowering  the  ex- 
haust pressure  15  pounds,  a  much  greater  gain  in  efficiency  is 
effected,  than  if  the  boiler  pressure  had  been  raised  50  pounds. 
Owing  to  the  fact  that  part  of  the  heat  is  lost  by  radiation, 
conduction,  cylinder  condensation,  leakage,  imperfect  valve 
action,  etc.,  the  efficiencies  herein  shown  are  never  realized  in 
the  actual  engine  or  turbine ;  the  calculation  Applies  to  a  perfect 
engine  only,  and  is  merely  for  comparison. 


Most  Economical  Vacuum  for   Steam   Engines 

It  has  been  definitely  proven  that  the  practical  vacuum 
suitable  for  reciprocating  engines  is  26  ",  and  there  is  no  economy 
in  carrying  a  higher  vacuum.  One  reason  for  this  is  that  in  the 
reciprocating  engine,  it  is  practically  impossible  to  take  full 
advantage  of  a  higher  vacuum  by  expanding  the  steam  in  the 
cylinder  down  to  the  condenser  pressure,  on  account  of  the-  ex- 
cessively large  volumes  of  steam  produced  by  expansion  to  lower 
pressures.  An  attempt  to  do  so  would  very  largely  increase 
the  bulk  of  the  engine  and  diminish  its  mechanical  efficiency. 
By  referring  to  the  steam  tables  on  pages  206-207,  one  can 
readily  see  how  rapidly  the  volume  increases  for  vacuums 
above  26  ". 

Even  if  it  were  found  practical  to  expand  to  a  lower  pres- 
sure than  2  pounds  absolute  (26 "  of  vacuum),  the  low  tem- 
perature of  the  exhaust  would  cool  the  cylinder  walls  to  such  an 
extent  as  to  cause  a  very  rapid  increase  in  cylinder  condensation. 

The  following  table  gives  an  idea  of  the  steam  consumption 
of  steam  engines  operating  condensing  and  non-condensing. 


173 


UNION       STEAM       PUMP       COMPANY 


Pounds   of   Dry   Steam   per  I.  H.  P.  per    Hour  at 
Full  Rated  Load 


I. 

H. 

P. 

Simple 
iigh  Speed 

Simple  Low  Speed 

Compound  High 
Speed 

Compound  Low 
Speed 

M 

a  e"" 

§o£ 
2.U-C 

M 

,  -S 

C  2 

si 

Non- 
Condensing 

Condensing 

Non 
Condensing 

Condensing 

Non- 
Condensing 

Condensing 

10 

65 

50 

- 

15 

57 

44 

20 

52.5 

40 

25 

49 

38 

30 

46.5 

36 

40 

42.5 

33 

50 

40 

30.2 

60 

38 

28.5 

75 

35.5 

26.2 

100 

33 

23.4 

27 

21.6 

29.3 

22.5 

23.6 

20 

150 

30.4 

21.5 

26.3 

21 

28.6 

22 

23.1 

19.5 

200 

29.5 

20.6 

25.7 

20.5 

27.9 

21.5 

22.7 

19 

250 

29 

20.2 

25.2 

20 

27.3 

21 

22.3 

18.5 

300 

28.5 

20 

24.8 

19.6 

26.6 

20.5 

21.9 

18.1 

400 

24.1 

18.8 

25.4 

19.5 

21.1 

17.3 

500 

23.7 

18.3 

24.2 

18.6 

20.4 

16.5 

600 

23.4 

17.9 

23.3 

17.9 

19.8 

15.8 

700 

23.2 

17.7 

22.7 

17.5 

19.2 

15.3 

800 

23 

17.6 

22.3 

17.2 

18.7 

15 

900 

22.9 

17.5 

22.1 

17 

18.4 

14.7 

1000 

22.8 

17.4 

22 

16.9 

18.2 

14.5 

1500 

13.8 

2000 

13.5 

2500 

13.2 

5000 

12.5 

ENGINEERING  OF  POWER  PLANTS. 

Most  Economical  Vacuum  for  Steam  Turbines 

For  steam  turbines,  the  average  practice  in  this  country 
as  well  as  abroad  is  to  employ  a  vacuum  of  28  "  referred  to  a  30  " 
barometer,  although  there  are  many  installations  under  1000 
K.  W. ,  which  operate  on  26  "  to  27  ",  and  others  of  larger  capacity, 
which  operate  on  28J4"  to  29  "  of  vacuum. 

There  is  a  tendency  on  the  part  of  steam  turbine  manu- 
facturers, because  of  the  obvious  advantages  of  steam  turbines 
over  reciprocating  engines  for  operating  at  high  vacuums,  to 
draw  attention  to  the  reduction  in  the  steam  consumption,  when 
a  plant  is  operated  at  high  vacuum.  The  question  is  raised 
whether  the  actual  economy  takes  into  consideration  the  increas- 


NG    MACHINERY,    AIR   COMPRESS 


ed  first  cost  of  the  condenser,  pumps,  and  piping,  together  with 
the  increased  operating  expense.  The  local  conditions,  parti- 
cularly the  temperature  of  the  cooling  water,  determine  this  to 
a  marked  degree.  In  locations  which  are  practically  at  sea  level, 
and  where  the  temperature  of  the  water  supply  for  the  con- 
denser is  very  low,  it  is  doubtless  profitable  to  install  condensing 
apparatus  of  sufficient  size  to  operate  steam  turbines  at  from 
28K"  to  29"  of  vacuum. 

The    following   table    gives    the    theoretical    and    practical 
vacuum  at  sea  level  for  varying  temperatures  of  cooling  water. 


Vacuum   At   Sea   Level   For  Varying  Tempera- 
tures of  Cooling  Water 


Temperature  of 
Cooling 
Water 
Deg.  Fah. 

Theoretical 
Possible 
Vacuum, 
Inches 

Perfect  Con- 
denser No  Temp. 
Difference 
Inches 

Actual  Con- 
denser 16"  Fah. 
Difference 
Inches 

Actual  Con- 
denser 15°  Fah. 
Difference 
Inches 

Ratio  Water 
to  Steam 

Infinite  Ratio 

60-1  Ratio 

60-1  Ratio 

100-1  Ratio 

32 

29.83 

29.67 

29.43 

29.54 

60 

29.50 

29.12 

28.56 

28.82 

70 

29.30 

28.73 

27.72 

28.38 

75 

29.10 

28  .  51 

27  .  37 

28.11 

J.   R.    BlBBINS 


In  modern  surface  condenser  installations,  there  is  usually 
a  difference  of  about  15°  Fah.  between  the  temperature  of  the 
condensed  steam  and  the  discharge  water.  It  will  be  seen  then, 
in  the  above  table,  that  with  a  reasonable  ratio  of  cooling  water 
to  the  steam  of  60  to  1,  the  maximum  vacuum  obtainable  when 
cooling  water  is  taken  at  60°,  is  28.6",  and  when  taken  in  at  70°, 
is  only  27.7  ". 

The  following  table  shows  the  actual  percentage  of  saving 
when  the  condensing  equipment  is  increased  so  a  plant  can  be 
operated  at  28"  of  vacuum,  instead  of  26 "  of  vacuum.  It  is 
estimated  that  the  cost  of  the  condensing  equipment,  including 
pumps  and  piping  will  be  $4000.00  more  for  a  2000  K.  W.  plant 
to  operate  at  28"  of  vacuum  than  at  26  inches  of  vacuum. 


175 


UNION       STEAM P  U  M  P       COM  PANY 


Relative  Economy  of  28"  of  Vacuum  Over  26"  of 
Vacuum  for  a  2000  K.  W.  Plant 

Increased   Cost   of  Equipment  is   $4000.00 


Net  Saving 
expressed  as 
Percentage  of 
Increased  Capi- 
tal Cost  to 
Secure  28"  of 
Vacuum  over 
that  for  26  *  of 

Average 
Load 
K.  W. 

Hours  of 
Service 
per  Day 

Actual 
Evapora- 
tion, 
Pounds 

Steam 
Consump- 
tion Aver- 
age Lbs. 
per  K.  W. 
Hotir 

Water 
Saved  per 
K.  W. 
Hour  by 
Raising 
Vacuum 
from  26" 

Cost  Coal, 
Dollars 
per  Ton 

Vacuum 

to  28" 

118 

1500 

24 

9.5 

23 

1.84 

4.50 

27 

1000 

24 

8 

22 

1.76 

2.25 

4 

1000 

10 

8 

22 

1.76 

1.13 

J.   R.    BlBBINS 

In  the  calculations,  the  rate  cf  interest  was  taken  at  5% 
and  depreciation  at  1%%  on  the  extra  equipment.  The  cost 
of  extra  power  consumed  was  at  the  rate  of  1  cent  per  K.  W. 
hour  and  10  cents  per  1000  gallons  of  feed-  water  saved. 

Although  it  may  be  stated  in  general  it  is  profitable  to  equip 
a  plant  to  operate  under  normal  conditions  at  a  vacuum  of  28 
inches,  there  are  cases  where  there  is  practically  no  saving  in 
so  doing.  In  the  third  case  given  above  where  the  plant  is 
working  on  a  ten  -hour  day,  and  coal  is  cheap,  the  gain  is  only 
4  per  cent. 

Operation  at  29  "  of  vacuum  compared  with  28"  is  not  so 
favorable  to  the  higher  vacuum  as  the  comparison  of  28  "  of 
vacuum  with  26  "  of  vacuum. 

It  will  be  observed  in  the  following  table  that  the  volume 
of  steam  is  increased  practically  in  the  same  ratio  (the  volume 
is  practically  doubled)  when  the  vacuum  is  increased  from  28" 
to  29  *,  as  when  increased  from  26  •  to  28  ". 


Table  of   the  Volume  of   a    Pound  (Specific   Vol- 

ume) of  Dry  Saturated  Steam  at 

High  Vacuums 


Vacuum 
29 
28 
26 


Volume  in  cubic  feet 

665 
342 
176 


In  the  above  table,  the  ratio  of  the  volume  at  28 "  vacuum 
to  that  at  26 "  vacuum  is  1.94,  and  the  ratio  of  the  volume  at 
29  "  of  vacuum  to  that  at  28  "  vacuum  is  1.95. 


PUMPING    MAcWlNlRiF  AIR 


A  v".r  :.•:• ..-'.  <;.::.  r,r..i 


176 


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The  capacity  of  the  condensing  equipment  for  a  steam 
turbine  operating  at  29  "  vacuum  must  be  practically  four  times 
as  large  as  would  be  required  for  one  exhausting  at  26  "  of  vacuum. 
In  other  words,  the  volume  of  a  pound  of  steam  at  the  exhaust  is 
166  cubic  feet  larger  at  28 "  of  vacuum  than  at  26"  of  vacuum, 
but  at  29 "  of  vacuum  it  is  323  cubic  feet  larger  than  at  28* 
of  vacuum.  It  has  already  been  shown  the  cost  of  condensing 
equipment  is  $4000.00  more  for  a  2000  K.  W.  unit  when  28" 
of  vacuum  is  substituted  for  26  "  of  vacuum,  and  hence  for  29 " 
of  vacuum,  the  cost  will  be  that  much  greater. 

For  turbine  installations  where  the  steam  consumption  is 
not  reduced  much  more  per  inch  of  vacuum  below  28-29" 
than  below  26-28"  in  a  comparison  of  economic  operation  at 
29  "  of  vacuum  with  28  ",  there  is  a  high  first  cost  for  condensing 
equipment,  which  is  not  offset  by  a  proportionate  reduction  in 
steam  consumption,  and  there  are  very  few  places  where 
an  installation  for  operation  at  an  average  vacuum  of  29"  is 
probable. 

An  idea  of  the  relative  quantity  of  the'  condensing  water 
required  for  different  vacuums  may  be  gained  by  comparing 
that  required  for  usual  operating  vacuums.  For  example, 
with  injection  water  at  70°  Fah.,  the  usual  temperature  upon 
which  condenser  guarantees  are  based,  it  is  customary  to  estimate 
that  to  obtain  a  vacuum  of  26"  referred  to  30"  barometer,  ap- 
proximately 26  pounds  of  water  will  be  required  for  each  pound 
of  steam  condensed,  and  approximately  2.5  times  this  quantity 
is  required  for  a  vacuum  of  28".  With  the  injection  water  at 
60°  Fah.,  which  should  be  considered  the  winter  temperature, 
the  quantity  required  for  the  foregoing  vacuums  is  approximately 
21  pounds  and  39  pounds  respectively.  Knowing  the  quantity 
of  the  condensing  water  required,  the  cost  of  fuel,  and  the  cost 
of  water  delivered  to  the  condenser,  the  vacuum  best  suited 
to  the  condenser  can  be  determined.  Theoretically,  the  effect 
of  operating  a  steam  turbine  by  reducing  the  vacuum  below 
that  for  which  it  is  designed  is  to  reduce  the  capacity  and  lower 
the  rating  at  which  the  maximum  economy  is  obtained. 

The  following  table  illustrates  the  percentage  gain  in  econ- 
omy per  inch  of  vacuum  for  various  vacuums.  The  close  agree- 
ment between  actual  results  and  theoretical  should  be  observed. 
This  table  applies  to  turbines  using  high  steam  pressures  and 
superheat. 


L.n.;ffiP  £5?ffP^^^ 

177 


UNION       STEAM       PUMP       COMPANY 


Gain  in  Per  Cent 


Inches  of  Vacuum 

28" 

27" 

26" 

25" 

Curtis  

5  1 

4  8 

4  6 

4  2 

Parsons  .        .                 .... 

5  0 

4  0 

3  5 

3  0 

Westinghouse-Parsons 

3  14 

3  05 

2  95 

2  87 

Theoretical  

5.2 

4.4 

3   7 

3  0 

Mech.  Eng.  Feb.  24,  1906. 

The  economy  in  operating  turbines  condensing  is  well  illus- 
trated in  the  following  tables,  which  give  the  results  of  tests  on 
a  300  K.  W.  and  a  500  K.  W.  turbine,  when  operating  condensing, 
and  non-condensing.  The  increase  in  steam  consumption  on  the 
300  K.  W.  turbine  is  about  50%  and  on  the  500  K.  W.  turbine, 
about  75%,  when  running  non -condensing. 


Test  of  a  300  K.  W.  Turbine 


K.  W. 

Steam  Pressure 
Gauge 

Superheat 
Degree  Fah. 

Vacuum 
Inches 

Pounds 
1C.  W.  Hour 

303 

158 

0 

26.58 

23.15 

297 

161 

0 

0 

34.20 

Tests  of  a  500  K.  W.  Turbine 


Brake  Horse 
Power 

Steam  Pressure 
Gauge 

Superheat 
Degrees  Fah. 

Vacuum 
Inches 

Pounds 
B.  H.  P/Hour 

383.5 

152  2 

.2 

28.2 

14.15 

755.6 

149.2 

1.2 

27.8 

13.28 

1121.9 

148.8 

5.1 

26.5 

14.32 

385.6 

148.2 

2.7 

8 

24   94 

766.8 

147.3 

2.6 

.8 

22.10 

1144.4 

126.1 

11.4 

.8 

24.36 

Steam  Consumption  of  Small  Steam  Turbines 

The  majority  of  small  steam  turbines  are  generally  operated 
non-condensing,  and  are  rated  on  the  brake  horse  powor.  Al- 
though the  steam  consumption  for  different  size  turbines  may 
vary  with  the  speed,  a  good  idea  of  the  steam  consumption  of 
non -condensing  units  may  be  secured  from  the  following  table: 


PUMPING    MACHINERY,    AIR    COMPRESSORS 


178 


Steam    Consumption    in    Lbs.   per   B.    H.    P.    per 

Hour  at  Full  Load,  150  Lbs.  Steam  Pressure. 

Atmosphere  Exhaust,  No  Back  Pressure 


Brake  Horse  Power 

Pounds  Steam  B.  H.  P.  per  Hour 

10 

60 

25 

50 

50 

45 

100 

40 

150 

35 

200 

30 

250 

28 

The  following  table  gives  the  comparative  figures  for  steam 
consumption  for  reciprocating  steam  engines  and  steam  turbines. 


Guaranteed  Steam  Consumption   Lbs.  per  K.  W* 
Hour,  150  Lbs.  Steam  Pressure 


K.  W. 

Compound  Corliss 
Steam  Engine, 
Saturated  Steam 

100°  Fah.  Superheat 

Steam  Turbine 
100°  Superheat 

Vacuum  26" 

Vacuum  28" 

500 

20. 

18    5 

18.1 

1000 

19.5 

18.0 

16.1 

1500 

18.5 

17.0 

15.8 

2000 

18.0 

16.50 

15.4 

AND    CONDENSERS    FOR    EVERT   S  ERVICE         1 

gTranrsorw^'y^r^y^r^ira^y^^iJ''!^!;^ 'uwww^np'ywwfi  ti  u  ii  ^  i  ^  L.  j  i  u ''..  i  ^  -  ^  i  i  L  i  i  *  u ^  L  u  u  *  ~i  \:  M  *  w  fw  i  M £ 


179 


I  O  N       STEAM 


PUMP 

OnanorfSlitSanCB: 


C  OMPANY 


Water   Rates  of  Turbo-Generators 


GO  CYCLE,  2300  VOLTS,  A.  C.  GENERATORS 


CONDENSING 


Steam  at  150  Lbs.  Gauge, 
28*  Vacuum 

Steam  at  200  Lbs.  Gauge, 
150°  Superheat,  29"  Vacuum 

Steam  at  150  Lbs.  Gauge 
Atmosphere  Exhaust 

Rating 
KW. 

Water  Rate  Lb.  per 
Hour  K.  W.,  includ- 
ing Excitation 

Rating 
K.  W. 

Water  Rate  Lb.  per 
Hour  per  K.  W. 
including  Excitation 

Rating 
K.W. 

Water  Rate    Lb. 
per  Hour  per  K.YV. 

50 

32       to  42 

4800 

12       to  13.3 

50 

52       to  60 

100 

21.2  to  27.5 

5000 

11.9  to  13 

100 

43.5  to  50 

200 

19.5  to  25 

7500 

11.6  to  12.6 

200 

38.4  to  44 

300 

18.7  to  22.5 

10000 

11.2  to  12.3 

300 

36.5  to  42 

400 

18.2  to  21 

12500 

11.1  to  12 

400 

35.2  to  40 

500 

17.7  to  19.3 

15000 

11.1  to  11.8 

500 

34.1  to  38 

600 

17.4  to  19 

17500 

11       to  11.6 

600 

33.4  to  37 

750 

17       to  18.8 

20000 

11       to  11  4 

750 

32.7  to  36 

1000 

16.5  to  18.6 

25000 

10.9  to  11.3 

1000 

31.7  to  35 

1250 

16.2  to  18.3 

30000 

10.8  to  11.2 

1250 

31       to  34 

1500 

16       to  18 

35000 

10.7  to  11.1 

1500 

30.7  to  33 

2000 

15.7  to  17.7 

40000 

10.6  to  11.1 

2000 

30.1  to  32 

250C 

15.5  to  17.4 

50000 

10.5  to  11 

2500 

29.4  to  31 

3000 
3500 

15.4  to  17.1 
15.3  to  16.9 

60000 
75000 

10.5  to  10.9 
10.4  to  10.8 

3000 
3500 

28.9  to  30 
28.6  to  29 

NON-CONDENSING 


Note.  —  Speeds  50-3500  K. 
K.  W.  inclusive,  1800  R.  P.  M 


LOEWENSTEIN 

W.  inclusive,  3600  R.  P.  M.,  4000  to  20000 
,  25000  K.  W.  and  over,  1200  R.  P.  M. 


180 


CRJEBK^     MICHIGAN.     U.  S.  A. 


Choice  of  Condensers 

The  choice  of  condensers  depends  almost  entirely  upon  the 
local  conditions,  particularly  the  nature  and  quantity  of  boiler 
feed  and  cooling  water  available.  For  vacuums  up  to  26 ", 
either  the  jet  condenser  or  the  surface  condenser  may  be  used. 
Where  a  high  vacuum  (26  "  to  29  ")  is  desired  in  connection  with 
a  steam  turbine  unit,  a  surface  condenser  is  generally  employed. 

Broadly  speaking,  condensers  may  be  divided  into  two 
classes:  (a)  those  in  which  the  cooling  water  is  mixed  with 
the  steam,  the  combined  quantities  being  discharged  to  the  hot 
well;  (b)  those  in  which  the  cooling  water  and  steam  to  be 
condensed  are  kept  separate,  the  cooling  water,  after  passing. 


•  MH«..  .B,..nB  „„ 


AND    C  Q  N  D  EN  S  E  R  S<    F  OR~EV  E  R  V  5  E  RV I C  E 


181 


I 


UNION       STEAM       PUMP       COMPANY 


through  the  condenser  being  either  discharged  to  waste,  or 
(by  means  of  suitable  cooling  arrangement  to  reduce  its  tem- 
perature) being  used  over  and  over  again  continuously,  while  the 
condensed  water  is  available  for  boiler  feed-.  To  class  (a) 
belongs  the  jet  condenser.  To  class  (b)  belong  the  surface  con- 
densers, vertical  or  horizontal,  counter-current,  or  parallel-cur- 
rent. 

In  the  marine  service,  jet  condensers  are  employed  only  on 
board  ships  operating  on  fresh  water.  Surface  condensers  with 
water  inside  of  the  tubes  and  steam  outside  are  universally  used 
on  board  ships  on  salt  water. 

In  land  practice,  the  jet  condenser  is  employed  where  there 
is  an  abundant  water  supply,  which  is  sufficiently  free  from 
impurities,  to  be  used  for  boiler  feed  on  account  of  its  relatively 
low  first  cost,  as  compared  with  surface  condensers.  However 
with  the  advent  of  the  steam  turbine,  which  requires  a  high 
vacuum,  the  surface  condenser  is  being  more  and  more  employed 
in  condenser  work. 

The  choice  of  condenser  will  obviously  depend  not  only  on 
the  quantity  of  the  water  available  for  condenser  purposes, 
but  also  upon  its  quality,  and  the  various  conditions  which  arise 
in  practice  might  be  met  as  follows: 

1.  An  abundant  supply  of  fresh  water,  sufficiently  pure  for 
boiler-feeding  purposes.     The  jet  condenser  would  be  the  most 
suitable  type  to  adopt. 

2.  An  abundant  supply  of  cheap  water,  but  of  a  quality 
unsuitable  for  boiler  feed.     It  is  desirable  to  use  a  surface  con- 
denser, and  if  the  boiler  feed  has  to  be  drawn  from  the  same 
source,  some  form  of  water  softening  or  purifying  plant;  or,  as 
the  case  of  marine  engines,  an  evaporator  becomes  necessary  to 
make  up  the  loss  of  feed  water  due  to  leakage. 

3.  A  limited  supply  of  water,  of  quality  right  for  boiler 
feed,  but  of  insufficient  quantity  to  be  discharged  to  waste, 
and  relatively  expensive  to  obtain.     A  jet  condenser  would  be 
the  best  to  adopt,  and  some  form  of  water  re-cooling  plant  be- 
comes necessary,  of  sufficient  capacity  to  reduce  the  tempera- 
ture to  a  point  low  enough  for  continuous  work. 

4.  A  limited  supply  of  water  unsuitable  for  bciler  feed.     A 
surface  condenser  would  be  the  most  suitable  type,  combined 
with  a  water-cooling  plant  of  ample  capacity  for  continuous  work, 
and  with  the   water  softening  or  purifying  apparatus  to  make 
up  the  loss  in  boiler  feed. 


182 


ft  «  »nar»nr»nr*  »  BUI  ffl  « 


B  A  T  T  LE      C  R.  E  E  K .     MI  CHIG  AN       U.  S.  A. 


Principles  of  Surface  Condensers 

The  important  factor  in  accomplishing  the  desired  results 
in  a  surface  condenser  is,  a  transference  of  heat  from  the  steam 
through  the  walls  of  the  tubes  to  the  cooling  water,  The  trans- 
ference of  heat  per  unit  of  area,  or  of  size,  is  a  measure  of  the 
efficiency  of  the  apparatus,  and  is  directly  proportional  to  the 
temperature  difference,  or  head.  In  a  surface  condenser,  the 
temperatures  of  the  fluids  are  different  at  different  parts  of  the 
surface.  The  temperature  of  the  circulating  water  increases 
during  its  passage  through  the  tubes,  becarse  of  the  absorption 
of  heat,  and  that  of  the  steam  decreases,  because  of  the  frictional 
drop  in  pressure.  It  is,  therefore,  necessary  to  obtain  mean 
values  for  temperature  differences. 

A  simple  arithmetic  mean  is  not  correct,  but  the  following 
formula  developed  mathematically  by  Grashof  has  been  proven 
in  practice  to  be  very  accurate,  and  is  used  very  extensively. 


T  —  T"  (39) 

TT  T  -*-  C  -*-    1  *  ' 

Hyp.  Log.-JL— -1 

1s       12 

Where  D  =Mean  temperature  difference 

T!  =The  lowest  temperature  of  the  fluid 
T2  =The  highest  temperature  of  the  fluid 
Ts  =The  temperature  of  the  gas  or  steam. 

(See  pages  206"  and  207.) 

In  modern  condenser  practice,  it  is  customary  to  make 
T2  10°  to  15°  less  than  Ts,  the  temperature  of  the  steam.  This 
factor  is  dependent  upon  the  design  of  the  condenser. 

Since  the  total  heat  to  be  abstracted  in  condensing  one 
pound  of  exhaust  steam  is  nearly  constant  within  practical 
ranges  of  vacuum,  it  is  apparent  that  the  maintenance  of  high 
vacuums  with  temperatures  rapidly  approaching  the  tempera- 
ture of  the  entering  cooling  water  requires  condensing  equipment 
of  much  larger  size  proportionately  than  indicated  by  the 
vacuum. 

Assuming  the  average  temperature  of  the  cooling  water 
as  70°  Fah. — heated  to  within  15°  of  the  temperature  of  the 
entering  steam,  then  a  surface  condenser  capable  of  condensing 
20,000  pounds  of  steam  per  hour  at  26 "  of  vacuum  will  con- 
dense approximately  only  14,000  pounds  at  a  vacuum  of  28", 
although  the  number  of  heat  units  required  per  pound  of  steam 


AND    C  O jj T)  E JN  S  JER  S >    F  Q >  R_  E ,  V E R .  Y  SE  RV I CB 

183 


Tl 

jj 


UNION.    STE  AM       P  U  MP       C  Q  M  PANY 

ifuvvwiliVVVVVVVVVWVVVVVIVVVVVVVVVIIWV^tVVVVVVVUVVVVWVVVVVlj^X^tSjLJllfllllvvfi 


is  practically  the  same  in  each  case.  The  explanation  of  this 
lies  in  the  value  of  the  mean  temperatures  difference,  which 
figures  from  the  formula  for  the  first  case  as  30.7°  Fah.  and  for 
the  last  case  as  22°. 

The  mean  temperature  difference  requires  for  a  maximum 
that  the  surfaces  be  arranged  for  counter-current  flow,  the  water 
entering  fartherest  from  the  steam  and  passing  consecutively 
through  the  tube  nests,  so  as  to  finally  pass  out  through  the 
entering  steam.  This  is  the  multi-pass  condenser  construction. 

The  transference  of  heat  through  a  unit  of  condenser  tube 
area  per  unit  of  mean  temperature  difference  was  early  recog- 
nized as  varying  greatly  under  different  conditions.  The  moct 
apparent  variation  being  an  increase  with  an  increase  in  the 
velocity  of  the  cooling  water.  Many  experimenters  have  carried 
out  exhaustive  tests  along  this  line  to  determine  the  most  practi- 
cal value,  but  the  results  obtained  vary  greatly  owing  to  the 
fact  that  in  practice  there  are  encountered  certain  resistances, 
which  are  in  addition  to  the  resistance  offered  by  the  metallic 
walls  of  the  tubes. 

The  transference  of  heat  produced  by  the  temperature 
head  is  opposed  by  the  resistance  of  the  metallic  walls  of  the 
tubes,  the  resistance  of  the  steam  side  of  the  tube  due  to  oil 
coating,  or  air -entrained  steam,  and  the  resistance  on  the  water 
side  of  the  tube  due  to  the  formation  of  scale. 

Among  the  metals  available  for  use  as  condenser  tubes, 
copper  is  of  the  highest  conductivity,  and,  furthermore,  when 
properly  alloyed,  is  less  subject  to  corrosion  than  most  others, 
thus  permitting  the  using  of  thinner  tubes.  Hence  all  condenser 
tubes  are  a  copper  ahoy.  The  size  of  tube  is  a  determining 
factor  in  the  thickness,  larger  tubes  require  greater  thicknesses 
for  mechanical  strength,  and  from  this  view  point  small  tubes 
are  desirable. 

To  prevent  the  formation  of  a  coating  of  oil  on  the  tubes, 
which  is  detrimental  to  the  heat  flow,  a  high  steam  velocity  must 
be  maintained  over  the  tubes,  and  there  must  be  no  dead  ends 
or  stagnant  places  in  the  condenser. 

To  eliminate  the  resistance  due  to  air-entrained  steam, 
surface  condensers  are  generally  arranged  so  that  the  steam 
sweeps  the  air  ahead  to  the  point  of  removal.  '  By  referring  to 
figures  82-83,  pages  202-203,  the  general  arrangement  of  a 
modern  high  vacuum  surface  condenser  can  be  seen,  which 


iE'RY,._AIR   CQMPJRJ&_S_S_ORS_        J 


184 


clearly  shows  the  counter-current  principle,  as  well  as  the  lo- 
cation of  the  circulating-water,  dry-air,  condensate,  and  exhaust- 
inlet  connections. 

The  resistance  on  the  water  side  of  the  tube  due  to  the 
formation  of  scale  is  very  important,  and  too  much  attention 
cannot  be  paid  to  keeping  the  tubes  clean.  A  high  circulating 
water  velocity  will  accomplish  this  to  a  marked  degree,  and  is  a 
more  important  reason  for  using  small  tubes,  and  several  passes, 
than  is  generally  recognized. 

The  coefficient  of  heat  transmission  or  B.  T.  U.  per  square 
foot  per  degree  difference  per  hour,  is  generally  taken  in  practice 
at  300  to  400,  depending  upon  the  degree  of  vacuum,  condenser 
design,  etc. 

Surface  Condenser  Calculations 

Cooling  Surface 

A  complete  equation  of  the  surface  condenser  is  as  follows: 

„    wx  Q      TT   w  xQ 

s=*nru or  u=*nrs         •        (40) 

U  =B.  T.  U.  per  square  foot  per  degree  difference  per  hour. 

M=Mean  temperature  difference  degrees  Fah. 

W  =  Pounds  of  steam  condensed  per  hour. 

S  =  Square  feet  of  cooling  surface. 

Q  =  Total  heat  removed  by  circulating  water  per  pound  of 
steam  condensed  (usually  taken  as  1000). 

The  table  on  page  204  gives  the  cooling  surface  required 
to  condense  1000  Ibs.  of  steam  per  hour  under  varying  conditions. 
This  table  has  been  calculated  by  equation  40,  and  is  based  on  a 
coefficient  of  heat  transmission  of  300  B.  T.  U.  per  square  foot 
per  degree  difference  per  hour. 

Cooling  Water 

In  calculating  the  amount  of  cooling  water  required  per 
pound  of  steam,  the  following  practical  equation  may  be  used: 

— Q 

(41) 

II  =  Total  heat  of  the  steam  (See  pages  206-207) 
Q  =Heat  of  the  liquid.     (See  pages  206-207) 
T2=  Final  temperature  of  the  cooling  water. 

(Generally  10°-15°  less  than  TJ 
T!  =The  initial  temperature  of  the  cooling  water. 


AND 

CON 

DEN 

SH 

RS 

FOR. 

H  V 

V    ,S 

FPV 

ICE 

=1 

185 


![        U  K  I  0  N 

STEAM 

PUMP 

COM  PANY 

3 

The  table  on  page  205  gives  the  cooling  water  required  for 
surface  condensers  for  vacuums  of  25 "  to  29 ".  This  table  has 
been  calculated  by  equation  41  for  cooling  water  temperatures  of 
50°  to  85°  Fah.,  and  for  temperature  differences  of  5°  to  20° 
between  the  temperature  due  to  the  vacuum  and  the  cooling 
water  discharge  temperature. 

Size  of  Auxiliaries 

In  calculating  the  size  of  pumps  to  use  with  a  surface  con- 
denser, the  following  gives  a  very  good  idea  of  customary  practice. 

Wet  air  pumps  used  in  connection  with  surface  condensers 
(without  dry  air  pumps)  for  26"  of  vacuum  and  less,  are  given  a 
displacement  of  20  times  the  volume  of  steam  condensed. 

The  condensate  pump  used  in  connection  with  a  surface 
condenser  (with  a  dry  air  pump) ,  is  generally  given  a  displacement 
of  2  to  3  times  the  volume  of  steam  condensed. 

With  regard  to  the  capacity  of  the  dry  air  pump,  the  following 
table  will  show  what  is  considered  good  practice. 

These  figures  are  based  upon  an  air  tight  system. 

Air  Pump  Displacement  per 
Vacuum  Pound  of  Steam  Condensed 

25  31 

26  37£ 

27  48 

28  55 
28^  60 

29  70 

Example 

Assume  we  have  500  K.  W.  steam  turbine  using  10,000  Ibs. 
of  steam  per  hour,  and  operating  on  28 "  of  vacuum.  It  is  re- 
quired to  find  the  size  surface  condenser,  the  amount  of  cooling 
water  at  70°  Fah.,  the  displacement  of  the  condensate  pump, 
and  the  displacement  of  the  dry  vacuum  pump  for  these  condi- 
tions. 

Solution 

1000  Ibs.  steam  per  hour  equals  2  gallons  per  minute. 
10,000  Ibs.  of  steam  per  hour  equals  20  gallons  per  minute. 

T2  =86.15°  (Assume  15°  lower  than  Ts.) 
Ts-101.15    (Seepage  206) 

The  mean  temperature  difference  from  equation  39,  sub- 
stituting the  above  values  equals : 

186 


86.15  —  70 
D  = 


101.15—70 
Hyp.  log. 


101.15—86.15 
16.15 


Hyp  log.  2.07 


.7275 
-22.2 

The  surface  of  the  condenser  may  now  be  calculated  from 
equation  40  by  substituting  the  values,  and  using  for  U  a  value 
of  300  B.  T.  U. 

10,000  X  1,000 
300  X  22.2 

=  1500  square  feet  of  cooling  surface 

The  amount  of  cooling  water  required  at  70°  Fah.,  is  calcu- 
lated from  the  equation  41  by  substituting  the  values  given 

_1104.1—  69.12 
86.15—70 

_  1034.98 
16.15 

=  64.1  pounds  of  cooling  water  per  pound  of  steam. 

Now  the  amount  of  steam  to  be  condensed  by  the  example 
is  10,000  Ibs.  per  hour,  or  20  gallons  per  minute,  so  the  amount 
of  cooling  water  required  to  condense  10,000  Ibs.  of  steam  per 
hour  will  be 

20  X  64.1  =1282  gallons  per  minute. 

The  displacement  of  the  condensate  pump  from  page  186, 
will  be 

20  X  3  =  60  gallons  per  minute. 

The  displacement  of  the  dry  vacuum  pump  from  page  186 
(for  28  "  of  vacuum)  ,  will  be 

-  =  148  cubic  feet. 
7.48 


187 


P     U  N  I  6  N 

STEAM 

PUMP 

C  OMPANY 

J 

c/3 


Jet  Condensers 

The  jet  condenser  consists  of  a  combination  of  condens- 
ing chamber  and  pump.  In  this  type  of  condenser,  the  condens- 
ing water  and  steam  come  in  direct  contact,  and  for  this  reason 
the  jet  condenser  is  particularly  well  adapted  for  use  where  the 
condensing  water  is  suitable  for  feeding  to  the  boilers.  A  sec- 
tional view  of  a  Burnham  jet  condenser  is  shown  in  figure  77. 
The  exhaust  steam  enters  at  A,  and  the  condensing  water  at  B. 
At  D  there  is  a  cone-shaped  spray  nozzle  connected  with  the 
tube  C.  The  water  issues  from  the  nozzle  D  in  an  umbrella- 
shaped  sheet  or  spray,  which  strikes  the  sides  of  the  condens- 
ing chamber  F.  Thus  the  steam  must  pass  through  or  into  the 
spray  on  entering  chamber  F  where  it  is  condensed.  The  mix- 
ture of  condensing  water  and  condensed  steam  descends  through 


PUMPING    MACHINERY,    AIR 


188 


|       BATTLE 

C 

RE 

EK. 

M 

ICH 

IG 

AN, 

U. 

S. 

A. 

; 

the  contracted  lower  end  of  the  condensing  chamber  Fin  a  solid 
stream,  which  insures  any  remaining  vapor  being  condensed, 
^hence  into  the  suction  of  the  pump,  which  discharges  the  water 
through  the  valves  T  and  opening  J  into  the  hot  well.  In  ad- 
dition to  discharging  the  mixture  of  condensed  steam  and  water, 
the  pump  removes  any  air  that  may  enter  in  the  injection  water 
or  through  leaks.  The  pump  also  raises  the  injection  water  used 
for  condensing  the  steam,  the  greatest  lift  being  generally 
twenty  feet.  At  E  is  a  hand  wheel  with  a  long  stem  connected 
to  the  movable  cone  D,  and  by  turning  this  wheel,  the  amount 
of  injection  water  may  be  regulated  to  suit  the  requirements. 


Fig.  77. 
Sectional  View  Through  Jet  Condenser 


b- 

AND 

CONDEN 

S 

ERS 

FOR 

EVERY  SERV 

res        : 

189 


[J        UNION 

STEAM 

P  UM  P 

c  b  Si  P  ANY    zj 

The  independent  steam  driven  type  of  jet  condenser  as 
illustrated  in  figure  77  has  the  advantage  of  being  absolutely 
independent  of  the  main  engine.  It  may  be  started  before 
and  stopped  after  the  main  engine,  thus  establishing  a  vacuum 
before  the  load  is  thrown  on  the  engine,  and  draining  the  pipes 
and  cylinder  of  the  water  of  condensation  and  leakage.  It  may 
be  run  at  any  speed  within  reason,  keeping  the  vacuum  constant 
under  changes  of  load. 

To  avoid  the  possibility  of  getting  water  over  into  the 
engine  cylinder  in  case  the  pump  stopped  while  the  engine  was 
running,  a  vacuum  breaking  device  is  arranged  in  the  condensing 
chamber,  as  it  is  illustrated  in  figure  77.  By  referring  to  this 
figure,  it  will  be  observed  that  in  case  the  pump  slows  down 
and  stops,  the  water  accumulating  in  the  condensing  chamber  F 
will  gradually  lift  the  float  G,  and  as  the  float  rises,  it  in  turn 
opens  the  air  valve  H,  admitting  air  to  the  exhaust  pipe  and 
engine  cylinder,  thus  breaking  the  vacuum.  This  equalizes 
the  pressure  in  the  condensing  chamber,  and  stops  the  flow  of 
the  injection  water.  The  engine  exhaust  will  then  accumulate 
until  it  acquires  sufficient  pressure  to  lift  the  atmospheric  relief 
valve,  and  the  engine  will  exhaust  into  the  atmosphere. 

In  starting  up  an  engine  with  a  jet  condenser  attached,  pro- 
ceed as  follows ;  open  slightly  the  injection  valve  D  and  start  up  the 
air  pump  to  its  normal  speed.  This  produces  a  vacuum  in  the 
pipes  and  condenser,  drains  them  of  all  water,  and  causes  the  in- 
jection water  to  flow  into  the  condenser.  When  the  vacuum 
is  established  as  shown  by  the  gauge,  open  the  throttle,  and 
turn  the  engine  over  slowly,  warming  it  up.  Then  bring  the 
engine  up  to  speed,  throw  on  the  load  and  regulate  the  amount 
of  injection  water  by  the  valve  D. 

The  wheel  E  on  the  top  of  the  condenser  is  used  for  regu- 
lating the  amount  of  injection  water.  The  speed  of  the  air 
pump,  and  the  amount  of  injection  water  must  be  regulated 
according  to  the  load  on  the  engine  and  the  vacuum  desired. 
When  shutting  down  an  engine  with  a  jet  condensing  apparatus, 
close  the  engine  throttle  first,  and  when  the  engine  is  stopped, 
and  not  until  then,  close  the  injection  valve  D,  and  lastly  shut 
down  the  air  pump.  By  shutting  off  the  water  supply  before 
the  air  pump  is  stopped,  the  water  already  in  the  condenser  and 
pipes  is  pumped  entirely  out,  and  there  is  no  danger  of  it  getting 
into  the  engine  cylinder. 


190 


C/3 


UNION       S  T  E  AM       PUMP     _C  O_M _P_ANY 


Table  Giving  Quantity  of  Injection  Water,  Vapors 

and  Pump  Displacement  for  Air  Pumps  and 

Jet  Condensers 


ll 

Temperature 

Temperature  of  Condensing  Water  at  Inlet 

Due 

to 
Vacuum 

Disch. 
Water 

50 

55 

CO 

65 

70 

75 

80 

85 

20 

161.4 

147 

W 
V 
S 
T 

10.8 
2.16 
5.4 
18.36 

11.1 

2.26 
5.4 

18.76 

12. 

2.4 
5.4 
19.8 

12.7 
2.54 
5.4 

20.64 

13.6 
2.72 
5.4 
21.72 

14.5 
2.9 
5.4 

22.8 

15.6 
3.12 
5.4 
24.12 

16.8 
3.3 
5.4 
25  5 

20% 

159 

144 

W 
V 

S 
T 

11.1 
2.34 
5.69 
19.13 

11.8 
2.49 
5.69 
19  98 

12.5 
2.63 
5.69 

20.82 

13.2 
2.78 
5.69 
21.67 

14.1 
2.97 
5.C9 
22.76 

15.2 
3.2 
5.69 
24.  C9 

16.3 
3.43 

26!  42 

17.7 
3.7 
5.6 
27.1 

21 

157 

141 

W 
V 

S 
T 

11.5 
2.5 

6 
20 

12.2 
2.64 
6 
20.84 

13 

2.8 
6 
21.8 

13.8 
2.98 
6 

22.78 

14.8 
3.2 
6 
21 

15.9 
3.44 
6 
25.  34 

17.2 
3.72 
6 
26.32 

18.7 
4.0 
6 

28.7 

>* 

154 

139 

W 
V 

S 
T 

11.8 
2.78 
6.35 
20.93 

12.5 
2.94 
6.35 
21.79 

13.3 
3.13 
6.35 

22.78 

14.2 
3.34 
6.35 
23.89 

U.3 

3.64 
6.35 
25.  29 

16.4 
3.86 
6.35 
26.61 

17.8 
4.19 
6.35 
28.34 

19.5 
4.5 
6.3 

30.4 

22 

152 

137 

W 
V 

S 
T 

12.1 
3 
6.75 

21  .  85 

12.6 
3.18 

6.75 
22.73 

13.7 
3.4 

6.75 
23.83 

14.  P 
3.63 
6.75 
21.98 

15.7 
3.9 
6.75 
26.35 

17 

4.22 
6.75 
27.97 

18.3 
4.55 
6.75 
29.60 

20.2 
5.0 
6.7 
31.9 

22% 

149 

134 

W 

V 
S 
T 
W 
V 
S 
T 

12.6 
3.36 
7.2 
23.16 

13.4 
3.57 
7.2 
24.17 

14.8 

3.81 
7.2 
25.31 

1.3.3 
4.08 
7.2 

26.  58 

16.5 
4.4 
7.2 
28.1 

17.9 
4.77 
7.2 
29.87 

19.6 
5.23 
7.2 
32.03 

21.6 
5.7 
7.2 
34.5 

23 

146.7 

132 

12.9 
3.7 
7.71 
24  31 

13.7 
3.92 
7.71 
25.33 

14.7 
4.21 
7.71 
26.62 

15.7 
4.5 
7.71 
27.91 

17.1 
4.9 

7.71 
29.71 

18.6 
5.33 
7.71 
31.64 

20.3 
5.82 
7.71 
33.93 

22.5 
6.4, 

7.7 
36.6 

23% 

143 

128 

W 
V 
S 
T 

13.6 

4.18 
8.31 
26.09 

14.5 
4.46 
8.31 
27.27 

15.6 
4.8 
8.31 
28.71 

16.9 
5.2 
8.31 
30.41 

18.3 
5.63 
8.31 
32.24 

20 
6.15 
8.31 
34.46 

22.1 
6.8 
8.31 
36.21 

24.7 
7.6 
8.3 
40.6 

24 

140.6 

126 

W 
V 
S 
T 

14 

4.67 
9 
27.67 

15 
5 
9 
29 

16.1 
5.34 
9 

30.44 

17.4 
5.77 
9 
32.17 

19 
6.3 
9 
34.3 

20.9 
6.93 
9 
36.  83 

23.1 
7.66 
9 
39.76 

26 
8.6 
9 
43.6 

24% 

137 

122 

W 
V 
S 
T 

14  8 
5.41 
9.82 
30.03 

15.9 
5.62 
9.82 
31.54 

17.2 
6.3 
9.82 
33.32 

18.7 
6.84 
9.82 
35.36 

20.5 
7.5 
9.82 
37.82 

22.7 
8.31 
9.82 
40.83 

25.4 
9.2 

9.82 
44.42 

28.9 
10.5 
9.8' 
49.25 

25 

133.7 

118 

W 
V 
S 
T 

15.8 
6.3 
10.8 
32.9 

17 

6.78 
10.8 
34.58 

18.5 

7.38 
10.8 
36.  68 

20.4 
8.06 
10.8 
39.06 

22.3 
8.9 
10  8 
42.0 

24.9 
9.93 

10.8 
45.63 

28.2 
11.26 
10.8 
50.26 

38.3 
15  25 
10  8 
56  2' 

35% 

129.7 

115 

W 
V 
S 
T 
W 
V 
S 
T 

16.5 
7.32 
12 
35.  82 

17.9 
7.94 
12 

37.84 

19.5 
8.65 
12 
40  15 

21.5 
9.54 
12 
43.04 

23.9 
10.6 
12 
46.5 

26.9 
11.93 
12 

50.83 

30.7 
13.61 
12 
56.  31 

35  8 
15  8' 
12 
63.6' 

26 

125.3 

110 

18 
9 
13.5 

40.5 

19.6 
9.8 
13.5 
42.9 

21.6 
10.8 
13.5 
45.9 

24 
12 
13.5 
49.5 

27 
13.5 
13.5 
54 

30.9 
15  5 
13.5 
59.9 

36 
18 
13.5 
67.5 

43.2 
21.6 
13.5 

78.3 

B  mi  n  «  nj.  «J»_«_«_^«J'  ««THMJ1»11AM1 ,«.»  U.  flLlLA^MUyb^BJjkJL^jnonraTr^TrBr^^ 

ING    MACHINERY.    AIR   COMPRESSORS 

«, .  i.  *^w^-^-ir^^tn^^rinrTinrtri,  u  -  v 


192 


Table  Giving  Quantity  of  Injection  Water,  Vapor 
and  Pump  Displacement  for  Air  Pumps  and 
Jet  Condensers 

(Continued") 


Vacuum 
Based  on 
30"  Barom. 

Temperature 

Temperature  of  Condensing  Water  at  Inlet 

Due 
to 
Vacuum 

Disch. 
Water 

90 

95 

100 

105 

lit 

115 

120 

30 

161.4 

147 

W 
V 
S 
T 

18.3 
3.66 
5.4 
27.36 

20.1 
4.02 
5.4 
29.52 

22.2 
4.44 

5.4 
32  04 

24.9 
4.98 
5.4 

35.28 

28.2 
5.64 
5.4 
39.24 

32.6 
6.52 
5.4 

44.52 

20% 

159 

144 

W 
V 

s 

T 

19.4 
4.08 
5.69 
29.17 

21.4 
4.51 
5.69 
31.60 

23.8 
5.01 
5.69 
34.50 

26.8 
5.64 
.  5.69 
38  13 

30.8 
6.49 
5.69 
43.98 

36.1 
7.6 

5.69 
49.39 

43.6 
9.18 
5.69 

58.47 

21 

157 

141 

W 
V 

s 

T 

50.6 
4.45 
6 
31.05 

22.8 
4.93 
6 
33.73 

25.6 
5.54 
6 
37.14 

29.1 
6.29 
6. 
'  41.39 

33.8 
7.04 
6 
46.84 

40.3 
8.72 
6 
55.02 

50 
10.8 
6 
66.8 

21% 

154 

139 

W 
V 
S 
T 

21.4 

5.04 
6.35 
32.79 

23.9 
5.62 
6.35 
35.  87 

26.9 
6.33 
6.35 
39.58 

30.9 
7.27 
6.35 
44.52 

36.2 
8.52 
6.35 

51.07 

43.8 
10.31 
6.35 

60  46 

55.3 
13.01 
6.35 

74  66 

22 

152 

137 

W 
V 

s 

T 

22  4 
5.57 
6.75 
34.72 

25.1 
6.23 
6.75 

38.98 

28.5 
7  08 
6.75 
42.33 

32.9 
8.17 
6.75 

47.82 

39 
9.69 
6.75 
55.44 

47.9 
11.9 
6.75 
66.  55 

61.9 
15.38 
6.75 

84.03 

22% 

149 

134 

W 
V 

s 

T 

24. 
6.4 
7.2 
37.6 

27.1 
7.23 
7.2 
41.53 

31 
8.27 
7.2 
49.47 

36.4 
9.71 
7.2 
53.31 

44 
11.73 
7.2 
62.33 

55.6 
14.83 
7.2 

77.63 

75.4 
20.11 
7.2 

102.71 

23 

146.7 

132 

W 
V 
S 
T 

25.2 
7.22 
7.71 
40.13 

28.6 
8.2 
7.71 
44.51 

33.1 
9.48 
7.71 
50.29 

39.2 
11.23 
7.71 

58.14 

48.1 
13.78 
7.71 
69.59 

62.2 
17.82 
7.71 
87.73 

88.2 
25.27 
7.71 

121.18 

23% 

143 

128 

W 
V 

s 

T 

27.09 
8.58 
8.31 
44.79 

32.2 
9.91 
8.31 
50.42 

37.9 
11.66 
8.31 

57.87 

46.2 
14.21 
8.31 
68.72 

59 
18.15 
8.31 
85.46 

81.7 
25.14 
8.31 
115.15 

132.7 
40.8 
8.31 
181  81 

24 

140.6 

126 

W 
V 

s 

T 

29.6 
9.82 
9. 

48.42 

34.3 
11.37 
9 
54.67 

40.9 
13.56 
9 
63.4fc 

50.7 
16.81 

/6.51 

66.5 
22.05 
9 
97.5"> 

96.7 
32.06 
9 
137.76 

177.3 
58.8 
9 
245.1 

24% 

137 

122 

W 
V 

s 

T 

33.4 
12.22 

9.82 
55.  44 

39.6 
14.49 
9.82 
63.91 

48.5 
17.74 
9.82 
76.06 

62.8 
22.98 
9.82 
95.60 

89 
32.56 
9.82 
131.38 

152.6 
55.83 
9.82 
218.25 

25 

133.7 

118 

W 
V 
S 
T 

38.3 
15.29 
10.8 
61.39 

46.6 
18.6 
10.8 
76.0 

5£.f 
23.8 
10.8 
94.2 

82.5 
32.93 

10.8 
126.23 

134 
53.43 
10.8 
198.28 

25% 

1297 

115 

W 
V 

s 

T 

43. 
19.03 
12. 
74.03 

53.8 
23.86 
12 
89.66 

71.7 
31.8 
12 
115.5 

107.5 
47.68 
12 
167.18 

215 
95.35 
12 

322.86 

26 

125.3 

110 

W 
V 

s 

T 

54. 
27. 
13.5 
94.5 

72 
36 
13.5 
121.5 

108 
54 
13.5 
175.5 

216 
108 
13.5 
337.5 

AND    CONDENSERS    FOR    EVERY  SERVICE 


193 


U  N 

I  0 

N 

S 

TE 

AM 

P 

UM 

P 

C 

OM 

PANY     Z| 

Fig.  79. 
Burnham  Air  Pump  and  Jet  Condenser 


Jet  Condenser  Factors 

The  preceding  table  gives  the  quantity  of  injection  water, 
the  volumes  of  vapor  with  the  steam  and  water,  and  the  displace- 
ment required  for  the  air  pump  with  jet  condensers  for  vacuums 
up  to  26 ",  and  using  condensing  water  from  50  to  120°  Fah.  The 
figures  are  calculated  from  the  formulae  42-43-44-45.  All 
figures  are  stated  in  multiples  of  condensed  steam. 

In  this  table 

W=  Quantity  of  condensing  water. 

V  =  Volume  of  vapor  from  the  water. 

S  =  Volume  of  vapor  from  the  steam  and  leaks. 

T  =(W  +  V  +  S)  =  Displacement  of  air  pump. 


BATTLE      CREEK.     MICHIGAN,,      U.S.A. 


Pumps  for  Jet  Condensers 

The  size  air  pump  to  use  with  a  jet  condenser  may  be  cal- 
culated by  the  following  formulae: 

(42) 


In  which  D  =  Displacement  of  pump. 

W=  Quantity  of  injection  water. 

2 
V=  Volume  of  vapors  from  water  =  —  XW  (43) 


54 
S  =  Volume  of  vapors  from  steam  and  leaks  =  —  X  Q  (44) 

*jn 

Pm  =  Absolute  pressure  inches  of  mercury. 

Q    =  Pounds  of  steam  to  be  condensed  per  hour. 

In  calculating  the  amount  of  injection  water,  let  H  be  the 
total  heat  in  one  pound  of  steam  at  the  terminal  pressure.  Ihis 
is  assumed  in  practice  at  1190  B.  T.  U.  • 

ts  =  Temperature  of  steam  due  to  the  vacuum. 

tl  =  Temperature  of  injection  water. 

t2  =  Temperature  of    discharge   water,  which  is  assumed  in 

practice  15°  lower  than  the     temperature  due  to  the 

vacuum. 

Each  pound  of  injection  water  will  be  heated  from  t±  to  t2, 
and  the  total  heat  absorbed  by  the  water. 

Hw=W(t2—  tO 
The  heat  given  up  by  the  steam  condensing  will  be 

HS=Q  (H—  12) 
Since  the  heat  absorbed  must  equal  that  given  up, 

W  (t2—  tO  =Q  (H—  12) 


(45) 


Example:  Given  12000  pounds  of  steam  per  hour  to  be 
condensed,  maintaining  26  "  of  vacuum,  referred  to  30  "  barometer 
using  70°  injection  water.  How  much  injection  water  is  required  ? 
What  size  air  pump  is  required? 


I  Or 


SERVICE 


195 


Solution : 

Q=  12000  Ibs. 

t!=70°. 

ts=125°  (see  page  207) 

t2=110° 

H=1190° 

Then  substituting  in  equation  45, 
12000  (1190—110) 


W  = 


110—70 
_  12000  X  1080 
40 

=  324000   pounds   of   injection   water   required   per 
hour. 

324000 

=648  G.  P.  M. 


8.3  X  60 

The  volume  of  vapors  from  the  water  equals  from  formula  43, 

2  2 

V=— XW=-X  324000 

Pm  4 

=  162000  pounds  per  hour  =324  G.  P.  M. 

The  volume  of  vapors  from  the  steam  and  leaks  equals 
from  formula  44, 

S=|         ^=13.5X12000 

m  i 

=  162000  pounds  per  hour  =324  G.  P.  M. 

Hence  from  equation  42,  the  displacement  of  the  air  pump 
must  equal 

D=  648 +  324 +  324  =1296  G.  P.  M. 

Now  referring  to  the  table  on  page  197,  you  will  find  that 
the  proper  size  air  pump  and  jet  condenser  for  these  conditions 
is  a  12x18x20,  which  has  a  condensing  capacity  of  12,300  pounds 
of  steam  per  hour,  and  a  displacement  of  1322  G.  P.  M. 

The  following  table  gives  the  sizes  of  air  pumps  and  jet 
condensers  for  various  amounts  of  steam  assuming  26  "  of  vacuum 
referred  to  30"  barometer,  and  using  cooling  water  at  50°  to  80° 
Fah.  The  quantity  of  cooling  water  required  for  these  condition  s 
is  also  given. 


!l^^ 

196 


C  R "E  E  K .     MICH  I  G  AN  , U.  S.  A. 


Air  Pumps  and  Jet  Condensers 


Size  Pump 

Strokes 
per 
Minute 

"!& 

l§| 

Steam  Condensed  per  Hour 
26"  Vacuum,  30"  Barometer 

Gallons  per  Minute 
Cooling  Water  Required 

Temp.  Cooling  Water 

Temp.  Cooling  Water 

5oii 

50° 

60° 

70° 

80° 

50° 

60° 

70° 

80° 

4£x  5x  8 

100 

68 

840 

740 

630 

500 

31 

32 

34 

36 

4^x  6x  8 

100 

98 

1200 

1070 

910 

730 

43 

46 

49 

53 

5  x  6x10 

100 

122 

1500 

1330 

1130 

910 

54 

58 

61 

66 

5  x  7x10 

100 

166 

2050 

1810 

1540 

1230 

73 

78 

83 

89 

6£x  8x10 

100 

217 

2700 

2380 

2000 

1610 

98 

103 

108 

116 

6£x  9x10 

100 

275 

3400 

3000 

2550 

2040 

122 

130 

138 

148 

6^x10x10 

100 

340 

4200 

3700 

3160 

2530 

152 

160 

170 

182 

8  x!0x!2 

100 

4C8 

5050 

4450 

3800 

3000 

180 

192 

205 

217 

8  x!2x!2 

100 

587 

7250 

6400 

5450 

4350 

260 

275 

290 

315 

8  xl2x!6 

75 

587 

7250 

6400 

5450 

4350 

260 

275 

290 

315 

10x14x16 

75 

800 

10000 

8750 

7400 

5950 

360 

375 

400 

430 

10x16x16 

75 

1044 

13000 

11400. 

9750 

7800 

470 

495 

525 

560 

12x16x20 

60 

1044 

13000 

11400 

9750 

78QO 

470 

495 

525 

560 

12x18x20 

60 

1322 

16400 

14400 

12300 

9800 

590 

625 

670 

710 

14x20x24 

50 

1632 

20000 

17700 

15000 

12000 

720 

765 

810 

870 

14x22x24 

50 

1974 

24400 

21500 

18300 

14600 

880 

930 

970 

1060 

14x24x24 

50 

2350 

29200 

25600 

21700 

17400 

1050 

1100 

1170 

1250 

16x26x24 

50 

2758 

34000 

30000 

25500 

20300 

1230 

1300 

1380 

1470 

16x28x24 

50 

3199 

40000 

35400 

30000 

23800 

1440 

1500 

1620 

1720 

16x30x24 

50 

3672 

45500 

40000 

34000 

27300 

1640 

1720 

1840 

1970 

Surface  Condensers 

In  a  surface  condenser,  figure  80,  the  steam  to  be  condensed, 
and  the  cooling  water  do  not  come  in  direct  contact  with  each 
other.  The  cooling  water  is  circulated  on  the  inside  of  a  series 
of  tubes,  and  the  steam  is  condensed  by  coming  in  contact  with 
the  outside  of  the  tubes.  The  condensed  steam  is  drawn  off 
by  the  air  pump.  The  condensing  water  is  drained,  or  forced 
through  the  tubes  by  the  circulating  pump.  The  external 
surface  of  the  tubes  which  comes  in  contact  with  the  steam  is 
the  condensing  surface 


197 


PUN 

I  ON 

STEAM 

P  UMP 

COM  PANY 

J 

Surface  condensers  usually  consist  of  a  cast  iron  shell,  or 
casing,  and  it  may  be  either  cylindrical  or  rectangular  in  form. 
The  cylindrical  form  is  the  simpliest  and  strongest  for  a  given 
sectional  area  and  weight  of  material,  is  cheaper  to  produce,  and 
is  considered  more  efficient  than  the  rectangular  type.  The  tube 
plates  may  be  of  cast  iron,  cast  brass,  or  Muntz  metal,  depending 
upon  the  installation.  In  the  marine  service,  condensers  are 
always  fitted  with  Muntz  metal  tube  heads. 


^ 


ATTLE      CREEK.     Ivi  I_Q  H  I  CAN ,      U.  g^  A. 


The  tubes  are  seamless  drawn  brass  (generally  60  copper 
and  40  zinc),  and  are  usually  made  ^"  external  diameter,  and 
No.  18-B.  W.  G.  in  thickness,  although  ^i"  external  diameter 
tubes,  and  either  18  B.  W.  G.  or  20  B.  W.  G.  are  sometimes  used. 


Fig.  81. 

The  tubes  are  secured  in  the  tube  plates  usually  by  means  of 
screwed  ferrules  and  tape  packing.  Figure  81  illustrates  the 
customary  method  of  securing  the  tubes  in  the  tube  plates  by 
screwed  ferrules.  It  will  be  noticed  the  ferrules  are  provided 
with  internal  lips  to  prevent  the  displacement  or  creeping  of  the 
tubes  by  giving  them  ample  room  to  expand  or  contract.  Some- 
times the  tubes  are  expanded  in  the  tube  plates,  but  this  method 
is  not  recommended  for  the  reason  that  a  certain  amount  of 
expansion  and  contraction  will  take  place,  which  tends  to  pro- 
duce slackness,  and  when  a  tube  has  become  slack,  it  is  a  diffi- 
cult matter  to  make  it  tight  again. 

The  condenser  shell  is  provided  with  one,  and  sometimes 
two  circulating  water  chambers,  depending  upon  the  number 
of  passes  in  the  condenser.  Suitably  arranged  cast-in  parti- 
tions in  the  circulating  water  chamber  and  heads  provide  for 
the  efficient  circulation  of  the  cooling  water  through  the  condenser 
tubes. 

Surface  condensers  are  built  in  the  horizontal  or  vertical 
types,  and  may  be  arranged  for  the  passage  of  the  cooling  water 
through  the  tubes  with  the  exhaust  steam  surrounding  them, 
or,  as  it  is  often  done  in  water-works  practice,  with  the  steam 
passing  through  the  tubes,  and  the  cooling  water  on  the  outside. 

A  baffle,  which  is  provided  opposite  the  main  exhaust 
steam  inlet  opening,  prevents  the  steam  from  eroding  the  outer 
row  of  tubes,  and  deflects  it  in  its  path  through  the  condenser. 

In  high  vacuum  surface  condensers,  drain  plates  are  fre- 
quently provided  to  intercept  the  condensed  steam  flowing 
through  the  condenser,  and  deflect  it  to  the  sides  and  bottom  of 
the  condensing  chamber,  so  as  to  keep  the  tubes  dry. 


,.J 


199 


L 

u 

N 

1  0 

N 

STE 

AM 

P 

U  M 

P 

COM  P  ANY 

J 

Surface  condensers  are  sometimes  made  with  a  single 
pass.  In  this  type,  the  cooling  water  enters  one  end  of  the 
condenser,  passes  through  the  tubes  once,  and  out  the  opposite 
head.  This  type  is  used  sometimes  for  installations  where  there 
is  a  large  amount  of  cooling  water  available,  and  a  high  velocity 
can  be  secured  through  the  tubes. 


In  two  pass  condensers,  as  is  shown  in  figure  82,  the  cooling 
water  enters  the  lower  side  of  the  circulating  water  chamber,  is 
deflected  by  the  dividing  partition,  and  flows  through  the  lower 
bank  of  tubes  to  the  opposite  end  of  the  condenser  into  the 
dished  head,  and  thence  returns  through  the  upper  bank  of 
tubes  and  on  the  top  of  the  circulating  water  chamber. 


Surface  condensers  are  made  with  as  many  as  three  and 
sometimes  more  passes,  depending  upon  conditions. 


Modern  surface  condensers  are  generally  designed  and  in- 
stalled so  that  the  steam  to  be  condensed  enters  horizontally 
at  the  side  near  the  top,  or  vertically  at  the  top  of  the  shell,  and 
in  condensing  flows  downward,  while  the  cooling  water  is  intro- 
duced at  the  bottom, and  leaves  at  the  top, thus  creating  a  counter- 
flow  of  the  two  fluids. 


The  condensate  is  removed  from  the  bottom  of  the  con- 
denser, and  with  high-vacuum  condensers  using  a  dry-air  pump, 
the  non-condensable  vapors  are  generally  drawn  off  from  the 
side  of  the  condenser. 


The  primary  functions  of  a  surface  condenser  are  to  reduce 
the  back  pressure  on  the  exhaust  side  of  a  steam  prime  mover; 
to  conserve  and  return  to  the  boiler  the  water  of  condensation, 
which  is  chemically  pure  feed  water;  to  conserve  and  return  to 
the  boiler  as  many  heat  units  as  possible;  and  to  remove  from 
the  feed  water,  the  air  in  solution,  thus  avoiding  pitting  of  the 
boilers. 


PUMP  IN  G    MAC  ^ 

200 


ATTLE      CREEK.     M  I C  H  I  G  AN,_  U.  S ._  A^^^, 


To  accomplish  these  results,  the  surface  condenser  must 
handle  four  separate  fluids:  steam,  air  (including  other  non- 
condensable  vapors),  water  of  condensation,  and  cooling  or 
circulating  water.  These  may  be  considered  separately  in  order 
to  reach  a  clear  understanding  of  the  subject.  As  the  desirable 
condition  or  state  of  these  several  fluids  is  not  the  same,  each 
installation  becomes  at  once  a  problem  to  be  carefully  con- 
sidered. In  dealing  with  these  fluids,  it  has  been  found  from 
practice  that  the  following  rules  must  be  observed  to  get  the  best 
results, 


The  steam  should  enter  the  condenser,  and  be  conducted 
freely  to  all  parts  of  the  same  with  the  least  possible  resistance ; 
it  should  be  reduced  to  the  lowest  practicable  temperature,  and 
should  be  converted  into  water  for  easy  removal. 


Air  which  is  a  nonconductor  of  heat  should  be  rapidly 
cleared  from  the  heat  transmitting  surfaces,  collected  at  suitable 
places  after  being  freed  from  the  entrained  water  and  vapor,  and 
cooled  to  a  low  temperature  of  removal  at  a  minimum  volume, 
and  consequently  a  minimum  expenditure  of  energy. 


The  condensate  should  also  be  rapidly  cleared  from  the 
heat  transmitting  surfaces,  freed  from  the  air,  collected  at  suit- 
able points  for  removal,  and  returned  to  the  boiler  at  the  maxi- 
mum temperature. 


The  circulating  water  should  pass  through  the  condenser 
with  the  least  friction,  deposit  a  minimum  amount  of  precipitate 
chemicals  and  absorb  a  maximum  amount  of  heat. 


201 


<N  _, 
00  *S 
.5?  ffi 


PUMPING    MACHINERY,    AIR 


I! 


202 


1 


AND    CONDENSERS*    FOR   EVERV  SERVICE 


203 


UNION 

STEAM 

P  UM  P 

COM  PANY 

Surface  to  Condense  1000  Pounds  Steam  Per 

Hour 


Vacuum 
Inches,  30" 
Barometer 

Temp. 
Rise  in 
Water  De- 
grees Pah  . 

Inlet  Water  Temperature  Degrees  Fah. 

50° 

55° 

60° 

65° 

70° 

75° 

80° 

85° 

5 

127 

153 

205 

295 

10 

139 

181 

29" 

15 

160 

220 

20 

196 

5 

89 

100 

116 

137 

170 

10 

90 

105 

125 

153 

202 

28%" 

15 

98 

115 

140 

180 

20 

108 

129 

164 

228 

25 

120 

150 

203 

5 

70 

75 

83 

99 

116 

144 

186 

10 

72 

82 

93 

108 

129 

162 

28" 

15 

78 

87 

101 

119 

149 

191 

20 

84 

95 

111 

135 

172 

25 

90 

104 

125 

159 

218 

30 

99 

116 

145 

198 

5 

57 

64 

70 

81 

93 

105 

126 

158 

10 

61 

69 

77 

85 

100 

116 

143 

21%" 

15 

65 

73 

81 

93 

110 

130 

163 

20 

69 

77 

88 

102 

121 

150 

197 

25 

74 

83 

96 

112 

138 

180 

30 

79 

90 

106 

128 

165 

5 

51 

58 

63 

70 

8(5 

87 

104   121 

10 

55 

61 

66 

74 

84 

96 

112 

135 

21" 

15 

58 

64 

71 

79 

90 

104 

124 

154 

20 

62 

.68 

75 

85 

97 

115 

141 

181 

25 

65 

72 

81 

92 

108 

130 

166 

30 

68 

77 

88 

101 

122 

155 

5 

49 

53 

57 

63 

.  69 

80 

87 

99 

10 

51 

55 

61 

66 

73 

83 

94 

110 

26%" 

15 

53 

58 

63 

71 

78 

89 

102 

122 

20 

55 

61 

67 

74 

84 

98 

115 

140 

25 

58 

64 

74 

80 

93 

108 

130 

167 

30 

61 

69 

79 

87 

100 

120 

153 

5 

45 

50 

54 

58 

63 

70 

80 

87 

10 

47 

51 

55 

61 

66 

74 

83 

97 

26" 

15 

49 

55 

59 

63 

71 

80 

90 

105 

20 

51 

54 

61 

67 

74 

84 

98 

116 

25 

54 

59 

65 

71 

80 

93 

108 

130 

30 

56 

62 

69 

77 

88 

100 

120 

154 

5 

40 

45 

46 

51 

53 

60 

~~~64~ 

73 

10 

43 

46 

50 

53 

58 

62 

68 

77 

25" 

15 

44 

47 

51 

55 

60 

65 

72 

82 

20 

45 

49 

53 

57 

62 

69 

78 

87 

25 

47 

51 

55 

60 

66 

74 

83 

96 

30 

50 

54 

58 

63 

71 

80 

90 

105 

PUMPING    MACHINERY, 


204 


COMPRES 


a 


Pounds  of  Cooling  Water  per  Pound  of 
Steam  Condensed. 


Vacuum 
Inches,  30 
Barometer. 

Temp, 
difference 
Degree 
Fah. 

Cooling  Water  Temperature  Deg.  Fah. 

50° 

55° 

60° 

65° 

70° 

75° 

80° 

85° 

29" 

6 
10 
12 
15 
18 
20 

45.7 
55.1 
61.8 
75 
95 

58.3 
75 
87.5 

80.8 

28V 

6 
10 
12 
15 
18 
20 

29.2 
32.8 
35 

38.9 
43.8 
47.8 

33.9 
38.9 
42 
47.8 
55.3 
62.2 

40.3 
47.8 
52.5 
62.2 
76 
88.9 

50 
62.2 
70.6 
89.0 

66.2 
89.0 

97 

28" 

6 
10 
12 
15 

18 
20 

23 
25.2 
26.5 

28.8 
31.2 
33.3 

25.8 
28.8 
30.2 
33.3 
36.6 
40 

29.5 
33.3 
35.5 
39.6 

44.7 
49 

34.5 
39.5 
43 
49 
57 
64.5 

41.3 
49 
54.5 
64.1 
79 

51.7 
64.5 
73.5 

69.5 

27%" 
27" 

6 
10 
12 
15 

18 
20 

19.6 
21.2 
22.2 
23.9 
25.3 
26.7 

21.6 
23.5 
24.7 
26.7 

28.8 
30.6 

24.5 
26.6 
28.2 
30.6 
33.5 
36.0 

27.6 
30.5 
32.5 
36.0 
40.3 
43.5 

31.8 
36.0 
38..  6 
43.5. 
50 
55.0 

37.2 
43.5 
47.5 
55.1 
65.7 
75 

45:3 

55.0 
61.8 
75 
96.0 

58.3 
75 
88.0 

6 
10 
12 
15 
18 
20 

17.8 
18.7 
19.4 
20.6 
21.8 
23.0 

19.2 
20.6 
21.4 
22.8 
24.5 
25.7 

21.0 
22.8 
24.0 
25.7 
27.8 
29.4 

23.2 
25.8 
27.1 
29.3 
32.2 
34.3 

26.4 
29.4 
31.2 
34.3 
38.0 
41.2 

30.3 
34.3 
36.7 
41.2 
46.7 
51.5 

35.5 

42 
44.7 
51.5 
60.8 
68.5 

42.9 
51.3 
57.0 
68.5 
85.5 

26%" 

6 

10 
12 
15 
18 
20 

16 
17 
17.5 
18.5 
19.6 
20.3 

17.3 
18.5 
19.2 
20.3 
21.5 
22.5 

19 
20.7 
21.3 
22.5 
24 
25.2 

21 
23 
23.5 
25.2 
27.3 
28.7 

23 
25.8 
26.5 
28.8 
31.5 
33.5 

26 
29.6 
30.5 
33.5 
37 
40 

30 
33.5 
35.6 
40 
45.3 
50 

35 
40 
43.5 
50 
58.3 
66 

26" 

6 
10 
12 
15 

18 
20 

14.8 
15.9 
16 
17.0 

17.8 
18.5 

16 
17.0 
17.5 
18.5 
19.5 
20.3 

17.2 
18.8 
19.2 
20.4 
21.6 
22.7 

19 
20.6 
21 
22.6 

24.4 
25.3 

21 
22.6 
23.8 
25.4 
27.5 
29. 

23 
25.4 
26.8 
29.0 
31.8 
33.7 

26 
29.2 
30.8 
34 
37.5 
40.3 

30 
33.7 
36.7 
40.3 
45.0 
50 

25" 

6 

10 
12 
15 
18 
20 

13.4 
13.6 
14.1 
14.6 
15.3 
15.7 

13.9 
14.6 
15 
15.7 
16.5 
17.1 

14.9 
15.7 
16.3 
17.3 
18 
18.7 

16.2 
17.1 
17.6 
18.7 
19.8 
20.6 

17.4 
18.7 
19.4 
20.6 
22 
23 

19.3 
20.6 
21.5 
23 

24.7 
26 

21.3 
23 

24.4 
26 
28.5 
30 

23.5 
26 
27.6 
30 
33.0 
35 

*Temperature  difference  between  that  due  to  saturated  steam  at 
any  particular  vacuum,  and  the  temperature  of  the  cooling  water  leaving 
the  condenser. 


205 


UN 

I  O  N 

STEAM 

P  UM  P 

COM  P  ANY 

3 

Properties  of  Saturated  Steam  at  Pressures  Less 
than  that  of  the  Atmosphere 


Vacuum  Inches 
Hg.  Referred  to 
30"  Barometer 
(Mercury  at 
58.4°  F.) 

Absolute 
Pressure 
in  Inches 
Mercury  at 
32°  P. 

Temp). 
Degrees 
Fahren- 
heit 

Specific 
Volume 
Cu.  Ft. 
per  Pound 

Heat 

of  the 
Liquid 

Total 
Heat 
of 

Steam 

Absolute 
Pressure 
in  Lbs. 
per  Sq. 
Inch 

29.8 

0.199 

34.42 

3004.0 

2.43 

1074.4 

0.097 

29.7 

0.299 

44.91 

2040.0 

12.97 

1079.2 

0.146 

29.6 

0.398 

52.60 

1554.0 

20.68 

1082  .  5 

0.195 

29.5 

0.498 

58.77 

1259.0 

26.85 

1085.3 

0.244 

29.4 

0.598 

63.86 

1063.0 

31.93 

1087.5 

0.293 

29.3 

0.698 

68.33 

918.0 

36.40 

1089.6 

0.342 

29.2 

0.797 

72.27 

810.0 

40.32 

1091.3 

0.390 

29.1 

0.897 

75  .  84  - 

724.0 

43.88 

1092.9 

0.439 

29.0 

0.997 

79.07 

657.0 

47.11 

1094.3 

0.488 

28.9 

1.097 

81.97 

599.3 

50.00 

1095.6 

0.537 

28.8 

1.996 

84.61 

552.5 

52.63 

1096.8 

0.586 

28.7 

1.296 

87.10 

512.2 

55.11 

1097.9 

0.635 

28.6 

1.396 

89.47 

476.9 

57.47 

1098.9 

0.684 

28.5 

1.495 

91.70 

446.2 

59.70 

1100.0 

0.732 

28.4 

1.595 

93.97 

419.6 

61.78 

1100.9 

0.781 

28.3 

1.695 

95.78 

396.0 

63  .  77 

1101.7 

0  .  830 

28.2 

1.795 

97.67 

375.0 

65.65 

1102.6 

0.879 

28.1 

1.894 

99.45 

356.4 

67.42 

1103.4 

0.928 

28.0 

1.994 

101.15 

339.6 

69.12 

1104.1 

0.977 

27.9 

2.094 

102.79 

324.1 

70.75 

1104.8 

1.026 

27.8 

2.194 

104.35 

310.3 

72.31 

1105.5 

1.075 

27.7 

2.293 

105.85 

297.6 

73  .  80 

1106.1 

1.123 

27.6 

2.393 

107.30 

286.0 

75.25 

1106.8 

1.172 

27.5 

2.493 

108.70 

275.2 

76.64 

1107.4 

1.221 

27.4 

2.592 

110.05 

265.1 

77.99 

1108.0 

1.270 

27.3 

2.692 

111.36 

255.8 

79.30 

1108.6 

1.319 

27.2 

2.792 

112.63 

247.2 

80.56 

1109.1 

1.368 

27.1 

2.892 

113.87 

239.2 

81.80 

1109.6 

1.417 

27.0 

2.991 

115.06 

231.9 

82.98 

1110.2 

1.465 

26.9 

3.091 

116.20 

224.6 

84.12 

1110  7 

1.514 

26.8 

3.191 

117.32 

218.0 

85.14 

1111.2 

1  .  563 

26.7 

3.291 

118.42 

211.7 

86.33 

1111.7 

.612 

26.6 

3.390 

119.50 

205  .  8 

87.41 

1112.2 

.661 

26.5 

3.490 

120  .55 

200.2 

88.46 

1112.6 

.710 

26.4 

3.590 

121.55 

195.1 

89.46 

1113.0 

.759 

26.3 

3.690 

122.54 

190.0 

90.44   " 

1113.4 

.808 

PUMPING    MACHINERY^    AIR   CONLPRES 


206 


r 

BATTLE 

C 

REE 

K. 

M 

ICH 

IGAN, 

U. 

s. 

A. 

1 

Properties  of  Saturated  Steam  at  Pressures  Less 
than  that  of  the  Atmosphere—  Continued 


Vacuum  Inches 
Hg.  Referred  to 
30"  Barometer 
(Mercury  at 
58.4°  F.) 

Absolute 
Pressure 
in  Inches 
Mercury 
at  32°  F. 

Temp. 
Degrees 

Fahren- 
heit 

Specific 
Volume 
Cu.  Ft. 
per  Pound 

Heat 

of  the 
Liquid 

Total 
Heat 
of 
Steam 

Absolute 
Pressure 
in  Lbs. 
per  Sq. 
Inch 

26.2 

3.789 

123.51 

185.5 

91.41 

1113.9 

1.856 

26.1 

3.889 

124.45 

181.0 

92.35 

1114.3 

1.905 

26.0 

3.989 

125.38 

176.7 

93.28 

1114.7 

1.954 

25.9 

4.088 

126.28 

172.7 

94.18 

1114.9 

9.003 

25.8 

4.188 

127.17 

1  68  .  9 

95.06 

1115.3 

2  .  052 

25.7 

4.288 

128.04 

165.1 

95.93 

1115.7 

2.101 

25.6 

4.388 

128.90 

161.5 

96.79 

1116.1 

2.150 

25.5 

4.487 

129.75 

158.1 

97.64' 

1116.5 

2.198 

25.4 

4.58 

130.59 

154.8 

98.48 

1116.9 

2.24 

25.3 

4.68 

131.42 

151.6 

99.30 

1117.3 

2.29 

25.2 

4.78 

132.21 

148.6 

100.11 

1117.7 

2.34 

25.1 

4.88 

133.00 

145.8 

100..88 

1118.0 

2.39 

25.0 

4.98 

133.77 

143.0 

101.65 

1118.3 

2.44 

24.0 

5.98 

140.64 

129.0 

108.51 

1121.3 

2.93 

23.0 

6.98 

146.78 

104.5 

114.64 

1123.9 

3.42 

22.0               7.97 

152.16 

92.3 

120.02 

1126.2 

3.90 

21.0 

8.97 

157.00 

82.6 

124.86 

1128.2 

4.39 

20.0 

9.97 

161.42 

74.8 

129.28 

1130.1 

4.88 

19.0 

10.97 

165.42 

68.5 

133.28 

1131.8 

5.37 

18.0 

11.96 

169.14 

63.1 

137.00 

1133.4 

5.86 

17.0 

12.96 

172.63 

58.6 

140.50 

1134.8 

6.35 

16.0 

13  .  96 

175.93 

54  6 

143.80 

1136.1 

6.84 

15.0 

14.95 

179.03 

51  .17 

146.91 

1137.4 

7.32 

14.0 

15.95 

181.92 

49.03 

149.80 

1138.6 

7.81 

13.0 

16.95 

184  .  68 

45.55 

152.57 

1139.7 

8.30 

12.0 

17.95 

187.31 

43.18 

155.21 

1140.7 

8.79 

11.0 

18.94 

189.83 

41.05 

157.73 

1141.7 

9.28 

10.0 

19.94 

192.23 

39.13 

160.14 

1142.3 

9.77 

9.0 

20.94 

194.52 

37.40 

162.44 

1143.6 

10.26 

8.0 

21.94 

196.73 

35.79 

164.68 

1144.5 

10.75 

7.0 

22.93 

198.87 

34.33 

166.81 

1145.4 

11.23 

6.0 

23.93 

200.94 

33.00 

168.88 

1146.3 

11.72 

5.0 

24.93 

202.92 

31.76 

170.89 

1147.0 

12.21 

4.0 

25.92 

204  .  85 

30.62 

172.81 

1147.6 

12.70 

3.0 

26.92 

206.71 

29.55 

174.68 

1148.4 

13.19 

2.0 

27.92 

208.52 

28.57 

176.50 

1149.1 

13.68 

1.0 

28.92 

210.28 

27.66 

178.27 

1149.7 

14.17 

0.0 

29.92 

212.00 

26.79 

180.00 

1150.4 

14.67 

1       AND 

CONDEN 

S 

ERS< 

FOR 

EVERY 

S 

ERVICE 

4 

STEAM       PUMP       COM  P  ANY 


Condenser  Auxiliaries 

With  a  jet  condenser,,  there  is  provided  an  air  pump  for 
removing  the  air  and  condensation,  and  generally  it  is  a  direct 
acting  steam  pump,  as  shown  in  figure  79,  page  194. 

The  injection  water  in  condensing  the  steam  in  a  jet  con- 
denser is  pumped  by  the  air  pump,  unless  the  source  of  supply 
is  far  distant,  in  which  case  a  centrifugal  or  direct-acting  pump 
is  used  for  pumping  the  supply. 

For  surface  condensers  operating  on  26  inches  vacuum  or 
less,  a  combined  air  and  circulating  pump  is  generally  provided 
as  shown  in  figure  84.  The  pump  consists  of  a  direct  acting 
steam  cylinder  with  an  air  cylinder  on  one  end  for  removing  air 
and  condensate,  and  a  circulating  cylinder  on  the  other  end, 
which  pumps  cooling  water  through  the  condenser.  The  con- 
denser may  be  mounted  on  the  pump  as  shown,  or  on  a  separate 
foundation,  and  piped  to  the  air  and  circulating  pump. 


Fig.  84. 
Surface  Condenser  Mounted  on  Air  and  Circulating  Pump 

Instead  of  a  combined  air  and  circulating  pump,  there  may 
be  provided  separate  pumps  for  handling  the  air  and  condensate. 
These  may  be  either  of  the  direct-acting  steam-driven,  or  cen- 
trifugal types. 

For  26"  of  vacuum«and  lower,  a  dry-air  pump  is  not  neces- 
sary, provided  a  wet  pump  is  used,  which  can  handle  both  the 
air  and  condensate. 

If  a  centrifugal  type  of  condensate  pump  is  used,  a  dry-air 
pump  is  necessary  to  remove  the  non-condensable  vapors,  as  a 
centrifugal  condensate  pump  can  handle  only  the  condensate. 


208 


For  vacuums  above  26 ",  surface  condensers  are  generally 
provided  with  circulating  pumps,  which  may  be  of  the  direct- 
acting  s  ceam-driven  type,  or  the  centrifugal  circulating  type. 


Fig-.  85. 
Burnham  Direct  Acting  Steam  Pump 

The  centrifugal  circulating  pump  is  especially  suitable  for 
this  service  on  account  of  its  simplicity,  and  saving  in  space  and 
weight.  It  may  be  belt  driven  or  operated  by  an  electric 
motor,  a  steam  turbine  or  a  vertical  steam-engine. 

Circulating  pumps  generally  operate  on  a  low  head  of  20-30 
feet,  and  this  head  consists  of  practically  all  friction  head  through 
the  condenser. 


Fig  86. 
Motor  Driven  Circulating  Pump 


209 


Fig.  87. 
Steam  Engine  Driven  Circulating  Pump 


Fig.  88. 
Steam  Turbine  Driven  Circulating  Pump 


The  condensate  pump  may  be  either  of  the  direct-acting 
type,  or  of  the  centrifugal  type. 

The  direct-acting  pump  has  not  been  much  used  since  the 
development  of  the  centrifugal  condensate  pump.  Centrifugal 
pumps  for  this  service  are  generally  small,  as  they  have  to 
handle  the  condensed  steam  only.  The  sizes  of  centrifugal 


condensate  pumps  generally  run  from 
is  sufficient  for  the  largest  units. 


to  6".     A  6"  pumi 


210 


BATTLE      CREEK.     MICHIGAN, U.S.A, 


Fig.  89 
Direct-Acting  Condensate  Pump 

Centrifugal  condensate  pumps  are  built  in  the  single  stage 
types,  either  motor,  or  turbine  driven.  The  head  is  rarely  over 
LO  feet,  of  which  approximately  30  feet  is  generally  due  to  the 
\  acuum  in  the  condenser,  and  the  remainder  friction  and  delivery 
head  in  the  discharge  line.  Centrifugal  pumps  should  always  be 
located  below  the  condenser,  so  that  there  is  a  head  of  approx- 
'mately  4  to  6  feet  on  the  pump. 


Fig.  193. 


Centrifugal  Condensate  Pump 

For  removing  the  non -con  den  sable  vapors,  a  dry-air  pump 
of  the  horizontal  reciprocating  type  is  provided  as  illustrated 
in  figure  91.  This  pump  may  be  steam  driven,  belt  driven,  or 
motor  driven,  depending  upon  conditions.  The  air  pump  is  a 
displacement  pump,  and  is  fitted  with  simple  flat  disc  air  valves 
located  in  the  ends  of  the  cylinder,  to  reduce  the  clearance.  A 


AND    CONDENSERS    FOR   EVERY  SERVICE 


211 


ii        U  N 

I  0  N 

STEAM 

P  UM  P 

by-pass  port  puts  the  two  ends  of  the  air  cylinder  in  communi- 
cation for  a  short  time  after  the  intake  and  discharge  valves 
are  closed  and  before  the  inlet  valves  open,  equalizing  the 
pressure  on  both  sides  of  the  piston,  and  a  voiding  part  of  the  loss 
due  to  expansion  of  the  vapor  in  the  clearance  spaces.  Recip- 
rocating air  pumps  are  very  economical  in  the  use  of  power. 
The  maximum  power  will  be  required  at  about  21 "  of  vacuum, 
and  decreases  as  the  vacuum  increases,  or  ^improves. 


Fig  91 
Steam  Driven  Dry  Air  Pump 

With  a  reciprocating  dry-air  pump,  the  pump  may  be 
started,  and  a  vacuum  created  in  the  condenser  without  the 
necessity  or  priming,  as  in  other  types  of  dry  air  pumps. 

Power  Required  by  Auxiliaries 

To  arrive  at  the  net  gain  in  economy  by  operating  a  steam 
engine  or  steam  turbine  condensing,  the  power  required  to 
operate  the  condenser  auxiliaries  must  be  charged  against  the 
initial  saving  in  steam  of  the  main  unit  produced  by  the  con- 
denser. With  the  jet  condenser,  this  power  is  what  is  required 
to  operate  the  air  pump,  and  in  the  case  of  the  surface  con- 
denser, it  is  the  power  required  to  operate  the  air  and  conden- 
sate  pumps,  as  well  as  the  circulating  pump. 

The  power  required  by  jet  condensers  varies  from  1  H.  P. 
per  1000  pounds  of  steam  used  per  hour  by  the  main  engine, 
in  the  case  of  large  units,  to  3  H.  P.  per  1000  pounds  of  steam 
for  small  units. 

The  power  required  by  the  auxiliaries  of  a  surface  condenser 
varies  from  2  to  5  per  cent  of  the  horse  power  of  the  main  unit. 

The  following  table  gives  the  approximate  power  required 
for  the  surface  condenser  auxiliaries  for  a  300,  500,  1000  and 
2000  K.  W.  turbine. 


PUMPING    MAC  MINE RY:   AIR   C O MP R ES^ORS^ 

BWW™^r^iT^«»V-g^^\ra-re^  u  t  w  *  v * •*. looSSaJ 


212 


BATTLE       C  R  E  EJtVl  M ".  ^H^I^^NT^V  ".S^T™ 


Power   Required   by  Auxiliaries    for   Surface 
Condensers 


K   W   on  Turbine  

300 
28" 
7000 

500 
23" 
10000 

1000 
28" 
20000 

2000 
26" 
30000 

Vacuum  

Steam  used  by  Turbine  per  Hr.  .  .  . 

Horse  Power  Used 

Circulating  Pump      

10 
4 
.  75 

3  .  05 

14 
6 
1 

3.12 

26 
12 
2 

30 

35 
18 
3 

2.1 

Dry  Air  Pump  

Condensate  Pump  . 

Per  cent  Power  of  Auxiliaries 
to  Power  of  Turbine  

Per  cent  Steam  used  by  Auxiliaries 
to  that  used  by  Turbines  

11.7 

11.0 

9.5 

9.0 

Fig.  84 

Burnham  Air  and  Circulating  Pump,  with  Surface  Condenser 
Mounted  on  Top 


SIZE  OP  PUMP 

, 

Diameter  of  Pump  Openings 

V 

3538, 

For  long  pipe  lines  use  larger  pioes, 

B 

a 

i  -O 

3  C 

B 

|  w§ 

reducing  size  at  pump  openings 

CO  - 

'o 

1 

oo 

,t  l  v-i 

O 

23 

CO 

^  s  o 

Air 

Pump 

Circulating 
Pump 

%   V. 

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ej 

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11 

15  *§ 

gj) 

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M 

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cd 

o 

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rt 

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rt  '^ 

M 

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y 

1 

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y 

01 

Po 

Po 

P^3 

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OS-SE 

CO 

W 

CO 

P 

CO 

P 

7 

8 

8 

10 

261 

4 

4 

4 

6 

5 

81A 

8 

9 

1J 

330 

Hi 

4 

4 

6 

6 

5 

8  J'i 

9 

9 

10 

330 

1  ^"2 

4 

4 

6 

5 

8 

10 

10 

12 

408 

1  Ji 

4 

4 

6 

5 

10 

10 

10 

12 

408 

M 

2 

4 

4 

6 

5 

10 

12 

12 

12 

587 

M 

2 

8 

5 

8 

6 

10 

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16 

587 

M 

2 

8 

5 

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6 

12 

14 

14 

12 

800 

14 

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ION       STEAM       PUMP       COMPANY 


Table  Showing  Weight  Per  Foot  of  Seamless 
Brass  Tubes 

Stub's  or  Birmingham  Gauge,  Measured  in  Outside  Diameters 


GAUGE  NO. 

3 

4 

5 

6 

7 

8 

9 

10 

11 

12 

13 

14 

Tnickness  of 
each    No.   in 
decimal  parts 

.259 

.238 

.220 

.203 

.180 

.165 

.148 

.134 

.120 

.109 

.095 

.083 

of  inch 

Frac.  of  inch 

• 

corresp'nding 

! 

15 

i3 

3 

11 

9 

! 

3 

5 

closely  to 

4 

64 

64 

1  6 

64 

6^T 

8 

32 

64 

G^uge   Nos.: 

Diameter 

'.»  .ibes,  In's. 



i:: 

.18 
.27 

.177 
.256 

.170 
.238 

.160 
220 

i 

.41 

.39 

.37 

.35 

.335 

.307 

.280 

A!; 

.52 

.49 

.47 

.  44 

.413 

.  376 

.  340 

i 

.70 

.66 

.64 

.60 

.57 

.53 

.492 

.444 

.400 

A.... 

.  84 

79 

76 

71 

66 

61 

571 

513 

.460 

1  .... 

1.09 

1.06 

.03 

.99 

.92 

.88 

.81 

.76 

.70 

.649 

.581 

.520 

i*.... 

1.28 

.23 

.19 

1.13 

1.05 

.99 

.92 

.86 

.79 

.728 

.650 

.580 

I  .... 

1.47 

.41 

.35 

1.28 

1.18 

1.11 

1.03 

.95 

.87 

.807 

.718 

.640 

If.  .  .  . 

1.65 

.58 

.50 

1.43 

.31 

1.23 

1.13 

1.05 

.90 

.885 

.787 

.700 

I.... 

1.84 

.75 

.66 

1.57 

.44 

1.35 

1.24 

.15 

1.04 

.964 

.855 

.759 

if.  ... 

2.03 

1.92 

.82 

1.72 

.57 

1.47 

1.35 

.24 

1.13 

1.042 

.924 

.819 

1    

2.22 

2.09 

.98 

1.87 

.70 

1.59 

1.45 

.34 

1.22 

1.12 

.99 

.88 

I  l/s.  .  .  . 

2.60 

2.44 

2.30 

2.16 

.96 

1.83 

1.67 

.53 

1.39 

1.28 

1.13 

1.00 

IX.'..'. 

2.97 

2.78 

2.61 

2.45 

2.22 

2.07 

1.88 

.73 

1.56 

.44 

1.27 

1.12 

iys.... 

3.35 

3.12 

2.93 

2.75 

2.48 

2.30 

2.10 

.92 

1.74 

1.59 

1.40 

1.24 

\1A.  .  .  . 

3.72 

3.47 

3.25 

3.04 

2.74 

2.54 

2.31 

2.11 

1.91 

1.75 

1.54 

1.36 

1%.  .  .  . 

4.09 

3.81 

3.57 

3.33 

3.00 

2.78 

2.52 

2.31 

2.08 

1.91 

.68 

1.48 

1%,  ... 

4.47 

4.15 

3.88 

3.62 

3.26 

3.02 

2.74 

2.50 

2.26 

2   06 

.82 

1.60 

ly8.... 

4.84 

4.50 

4.20 

3.92 

3.52 

3.26 

2.95 

2.69 

2.43 

2.22 

.95 

1.72 

2      .... 

5.21 

4.84 

4.52 

4.21 

3.78 

3.50 

3.16 

2.89 

2.60 

2.38 

2.09 

1.84 

1K.-.T. 

5.59 

5.18 

4.84 

4.50 

4.04 

3.73 

3.38 

3.08 

2.78 

2.54 

2.23 

1.96 

2M.... 

5.96 

5.53 

5.15 

4.80 

4.30 

3.97 

3.59 

3.27 

2.95 

2.69 

2.36 

2.08 

2^.  ... 

6.34 

5.87 

5.47 

5.09 

4.56 

4.21 

3.80 

3.47 

3.12 

2.85 

2.50 

2.20 

2H-  •  •  • 

6.71 

6.21 

5.79 

5.38 

4.82 

4.45 

4.02 

3.66 

3.30 

3.01 

2.64 

2.32 

2%.  ... 

7.08 

6.56 

6.11 

5.67 

5.08 

4.69 

4.23 

3.85 

3.47 

3.17 

2.77 

2.44 

25*.... 

7.46 

6.90 

6.42 

5.97 

5.34 

4.92 

4.44 

4.05 

3.64 

3.32 

2.91 

2.56 

*«.... 

7.83 

7.24 

6.74 

6.26 

5.60 

5.16 

4.66 

4.24 

3.81 

3.48 

3.05 

2.68 

3     

8.20 

7.59 

7.06 

6.55 

5.86 

5.40 

4.87 

4.43 

3.99 

3.64 

3.19 

2.79 

3H-  •  •  • 

8.58 

7.93 

7.38 

6.85 

6.12 

5.64 

5.08 

4.63 

4.16 

3.79 

3.32 

2.91 

3M.... 

8.95 

8.27 

7.69 

7.14 

6.38 

5.88 

5.30 

4.82 

4.33 

3.95 

3.46 

3.03 

3^8  

9.33 

8.62 

8.01 

7.43 

6.64 

6.11 

5.51 

5.01 

4.51 

.11 

3.60 

3.15 

3^  

9.70 

8.96 

8.33 

7.72 

6.90 

6.35 

5.72 

5.21 

4.68 

.27 

3.73 

3.27 

*;«.... 

10.07 

9.30 

8.65 

8.02 

7.16 

6.59 

5.94 

5.40 

4.85 

.42 

3.87 

3.39 

*«.... 

10.45 

9.65 

8.96 

8.31 

7.42 

6.83 

6.15 

5.59 

5.03 

.58 

4.01 

3.51 

3Ji.... 

10.82 

9.99 

9.28 

8.60 

7.68 

7.07 

6.37 

5.79 

5.20 

.74 

4.15 

3.6? 

To  determine  weight  per  foot  of  a  tube  of  a  given  Inside 

Diameter,  add  to  weights  in  above  list  the  weights  given 

below  under  corresponding  gauge  numbers 


GAUGE  NO.    |      3 

4 

5 

6 

7 

8 

9 

10 

11 

12 

13 

14 

Increase  in    I 
ibs.  per  foot|i.5487 

1.3077 

1.1174 

.951! 

.7480 

.6285 

.5057 

.4145 

.3324 

.2743 

.2084 

.1590 

218 


Table  Showing  Weight  per  Foot  of  Seamless 
Brass  Tubes 

(Continued) 

Stub's  or  Birmingham  Gauge,  Measured  in  Outside  Diameters 


GAUGE  NO. 

15 

16 

17 

18 

19 

20 

21 

22 

23 

24 

25 

26 

27 

1  nickness  of 
;ach    No.   in 
decimal  parts 

.072 

.065 

.058 

.049 

.042 

.035 

.032 

.028 

.025 

.022 

.020 

.018 

.016 

of  inch: 

Frac.  of  inch 

correspondi'g 

! 

3 

i 

i 

closely  to 

16 

64 

32 

64 

Gauge  Nos.: 

Diameter 

Tubes,  In's 

*.... 

.045 

.045 

.043 

.040 

.036 

.034 

.031 

.029 

.026 

.024 

.022 

.020 

i% 

.096 

.092 

087 

.078 

.070 

.062 

.057 

.051 

.047 

.042 

.039 

.035 

032 

i.... 

.148 

.139 

.129 

.114 

.101 

.087 

.080 

.072 

.065 

.058 

.053 

.048 

.043 

A 

.200 

.186 

.170 

.149 

.131 

.112 

.104 

.092 

.083 

.074 

.067 

.061 

.055 

t: 

.252 

.233 

.212 

.184 

.161 

.137 

.127 

.112 

.101 

.090 

.082 

.074 

.066 

A.... 

.304 

.279 

.254 

.220 

.192 

.163 

.150 

.132 

119 

.106 

.096 

.087 

.078 

I 

.356 

.326 

.296 

.255 

.222 

.188 

.173 

.152 

.137 

.121 

.111 

.100 

.089 

A;'- 

.408 

.373 

.338 

.290 

.252 

.213 

.196 

.173 

.155 

.137 

.125 

.US 

.101 

i.... 

.460 

.420 

.380 

.326 

.283 

.238 

.219 

.193 

.173 

.153 

.140 

.126 

.112 

«.  .  .  . 

.511 

.467 

.421 

.361 

.313 

.264 

.242 

.213 

.191 

.169 

.154 

.139 

.124 

I...;,. 

.563 

.514 

.463 

.396 

.343 

.289 

.265 

.233 

.209 

.185 

.169 

.152 

.136 

H 

.615 

.561 

505 

.432 

.373 

.314 

.288 

.25*3 

.227 

.201 

.183 

.165 

.148 

i  !  '.  '.'. 

.667 

.608 

.547 

.467 

.404 

.339 

.311 

.274 

.245 

.217 

.197 

.178 

.159 

H.... 

.719 

.655 

.589 

.502 

.434 

.365 

.334 

.294 

.263 

.232 

.211 

.191 

.171 

i    .... 

.77 

.70 

.63 

.54 

.46 

.389 

.358 

.314 

.281 

.248 

.226 

.204 

.182 

lH- 

.87 

.79 

.71 

.61 

.52 

.439 

.404 

.354 

.317 

.280 

.255 

.23( 

.205 

1M. 

.98 

.89 

.80 

.68 

.59 

.490 

.450 

.395 

.354 

.312 

284 

.25G 

.228 

1%.  ... 

1.08 

.98 

.88 

.75 

.65 

.540 

.496 

.435 

.390 

.343 

•  .313 

282 

.251 

l^A. 

.19 

1.08 

.96 

.82 

.71 

.591 

.542 

.476 

.426 

.375 

.342 

.308 

.274 

i^.  ... 

.29 

1.17 

1.05 

.89 

.77 

.641 

.588 

.516 

.462 

.407 

.371 

.334 

i?i.... 

.39 

1.26 

1.13 

.96 

.83 

.692 

.635 

.556 

.498 

.439 

.399 

.360 

ij-6  .  .  .  . 

.50 

1.36 

.22 

.03 

.89 

.742 

.681 

.597 

.534 

.470 

.428 

.386 

2 

.60 

.45 

30 

..10 

.95 

.793 

.727 

.637 

.570 

.502 

.457 

412 

.71 

.55 

.38 

.17 

.01 

.843 

.773 

.678 

.606 

.534 

.486 

2M- 

.81 

.64 

.47 

.24 

.07 

.894 

.819 

.718 

.642 

.566 

.515 



2^.... 

.91 

.73 

.55 

.32 

.13 

.944 

.866 

.758 

.678 

.597 

544 

•  .  . 

2.02 

.83 

.63 

.39 

.19 

.995 

.912 

.799 

.714 

.629 

.573 

2H-.V 

2.12 

.92 

.72 

.46 

.25 

1.045 

.958 

.839 

.750 

.661 



25*.... 

2.23 

2.01 

.80 

.53 

.31 

1.096 

1.004 

.880 

.786 

.693 



aft.:..* 

2.33 

2.11 

.89 

.60 

.37 

1.146 

1.050 

.920 

.822 

.724 



3     .... 

2.43 

2.20 

.97 

.67 

.43 

1.197 

1.096 

.960 

.859 

.756 



31^ 

2.  54 

2.  30 

2.05 

74 

.49 

1.  247 

1.143 

1.  001 

.895 

.788 

O  78  •   •   •   • 

3)*  

2.64 

2.39 

2.14 

.81 

.55 

1.298 

1.189 

1.041 

.931 

.820 

33% 

2.  74 

2.48 

2.  22 

.88 

1.62 

1.  348 

1.235 

1.082 

.967 

.  851 

o  7^8  .... 

2.  85 

2.  58 

2.  30 

1.  95 

1.68 

1.  399 

1.  281 

1.122 

1.003 

.883 

3^ 

2.  95 

2.  67 

2.  39 

2.  02 

1.74 

1.449 

1.  327 

1.  162 

1.039 

.915 

q3/ 

3.06 

2.  76 

2.47 

2.  09 

1.  80 

1.50 

1.  373 

1.  203 

1.075 

.946 

3%.... 

3.16 

2.86 

2.56 

2.16 

1.86 

1.55 

1.42 

1.243 

1.111 

.978 

To  determine  weight  per  foot  of  a  tube  of  a  given  Inside  Diameter, 
add  to  weights  in  above  list  the  weights  given  below  under 
corresponding  gauge  numbers. 


GAUGE  NO. 

15 

16 

17 

18 

19 

20 

21 

22 

23 

24 

25 

26 

27 

Increase  in 
Ibs.  per  foot: 

.1197 

.0975 

.0777 

.0554 

.0407 

.0283 

.0236 

.0181 

.0144 

.0112 

.0092 

.0075 

.0059 

1 


AND   CONDENSERS    FOR   EVERT  SERVICE 


219 


Table  Showing  Weight  Per  Foot  of  Seamless 
Brass  Tubes 

(Continued) 

Stub's  or  Birmingham  Gauge,  Measured  in  Outside  Diameters 


GAUGE  NO. 

3 

4 

5 

6 

7 

8 

9 

10 

11 

12 

Thickness  of  each 
ISo.  in  decimal 
parts  of  inch 

.259 

.238 

.220 

.203 

.180 

.165 

.148 

.134 

.120 

.109 

Fraction  of  inch, 
corresponding  closely 
to  Gauge  Nos.: 

i 

4* 

M 

A 

ft 

& 

ir" 

Diameter  Tubes, 
Inches 

4      

0*  
4M  

4^ 

11.19 
11.57 
11.94 
12.32 
12.69 
13.06 
13.44 
13.81 
14.18 
14,56 
14.93 
15.31 
15.68 
16.05 
16.43 
16.80 
17.17 
17.55 
17.92 
18.30 
18.67 
19.04 
19.42 
19.79 
20.16 
20.54 
20.91 
21.29 
21.66 
22.03 
22.41 
22.78 
23.15 

10.33 
10.68 
11.02 
11.36 
11.71 
12.05 
12.39 
12.74 
13.08 
13.42 
13.77 
14.11 
14.45 
14.80 
15.14 
15.48 
15.83 
16.17 
16.51 
16.86 
17.20 
17.54 
17.89 
18.23 
18.57 
18.92 
19.26 
19.60 
19.95 
20.29 
20.64 
20.98 
21.32 

9.60 
9.91 
10.23 
10.55 
10.87 
11.18 
11.50 
11.82 
12.14 
12.45 
12.77 
13.09 
13.41 
13.72 
14.04 
14.36 
14.67 
14.99 
15.31 
15.63 
15.94 
16.26 
16.58 
16.90 
17.21 
17.53 
17.85 
18.17 
18.48 
18.80 
19.12 
19.44 
19.75 

8.90 
9.19 
9.48 
9.77 
10.07 
10.36 
10.65 
10.95 
11.24 
11.53 
11.82 
12.12 
12.41 
12.70 
13.00 
13.29 
13.58 
13.87 
14.17 
14.46 
14.75 
15.05 
15.34 
15.63 
15.92 
16.22 
16.51 
16.80 
17.10 
17.39 
17.68 
17.98 
18.27 

7.94 
8.20 
8.46 
8.72 
8.98 
9.24 
9.50 
9.76 
10.02 
10.28 
10.53 
10.79 
11.05 
11.31 
11.57 
11.83 
12.09 
12.35 
12.61 
12.87 
13.13 
13.39 
13.65 
13.91 
14.17 
14.  4S 
14.69 
14.95 
15.21 
15.47 
15.73 
15.99 
16.25 

7.31 
7.54 
7.78 
8.02 
8.26 
8.50 
8.73 
8.97 
9.21 
9.45 
9.69 
9.92 
10.16 
10.40 
10.64 
10.88 
11.12 
11.35 
11.59 
11.83 
12.07 
12.31 
12.54 
12.78 
13.02 
13.26 
13.50 
13.73 
13.97 
14.21 
14.45 
14.69 
14.93 

6.58 
6.79 
7.01 
7.22 
7.43 
7.65 
7.86 
8.07 
8.29 
8.50 
8.71 
8.93 
9.14 
9.35 
9.57 
9.78 
9.99 
10.21 
10.42 
10.64 
10.85 
11.06 
11.28 
11.49 
11.70 
11.92 
12.13 
12.34 
12.56 
12.77 
12.98 
13.20 
13.41 

5.98 
6.17 
6.37 
6.56 
6.75 
6.94 
7.14 
7.33 
7.53 
7.72 
7.91 
8.11 
8.30 
8.49 
8.69 
8.88 
9.07 
9.27 
9.46 
9.65 
9.85 
10.04 
10.23 
10.43 
10.62 
10.81 
11.01 
11.20 
11.39 
11.59 
11.78 
11.97 
12.17 

5.37 
5.55 
5.72 
5.89 
6.06 
6.24 
6.41 
6.58 
6.76 
6.93 
7.10 
7.28 
7.45 
7.62 
7.80 
7.97 
8.14 
8.32 
8.49 
8.66 
8.84 
9.01 
9.18 
9.35 
9.5S 
9.70 
9.87 
10.05 
10.22 
10.39 
10.57 
10.74 
10.91 

4.89 
5.05 
5.21 
5.37 
5.52 
5.68 
5.84 
6.00 
6.15 
6.31 
6.47 
6.62 
6.78 
6.94 
7.10 
7.25 
7.41 
7.57 
7.72 
7.88 
8.04 
8.20 
8.35 
8.51 
8.67 
8.83 
8.98 
9.14 
9.30 
9.45 
9.61 
9.77 
9.93 

4H 

4!H? 

4^  

43^  ...   . 

5     .... 

51^  

5J£  

5^  

5H  

9$4 

5%  

5y8...... 

Q         

61$  

6M  
63A  
6H  

6^ 

65^  ... 

6^   ...    . 

7     

7H  
7H  
7^  

m 

iy*    .  . 

7%  

7%  

8     

To  determine  weight  per  foot  of  a  tube  of  a  given  Inside  Diameter, 

add  to  weights  in  above  list  the  weights  given  below  under 

corresponding  gauge  numbers. 


GAUGE  NO. 

3 

4 

5 

•:, 

I 

8 

9 

10 

11 

12 

Increase  m  Pounds 
Per  Foot 

1.5487 

1.3077 

1.1174 

.9514 

.7480 

.6285 

.5057 

.4145 

.3324 

.2743 

220 


UA 

ATTLE 

C 

RE 

E 

K. 

MIC 

HIG 

AN. 

U. 

S. 

A.       : 

Table  Showing  Weight  per  Foot  of  Seamless 
Brass  Tubes 

(Continued) 

Stub's  or  Birmingham  Gauge,  Measured  in  Outside  Diameters 


GAUGE  NO. 

13 

14 

15 

16 

17 

18 

19 

20 

21 

22 

23 

24 

Thickness   of 
each    No.  in 
decimal  parts 
of  inch: 
Frac.  of  inch 
correspondi'g 
closely  to 
Gauge  No».: 

.095 

.083 

.072 

.065 

.058 

.049 

.042 

.035 

.032 

.028 

.025 

.022 

& 

A 

A 

A 

A 



Diameter 
Tubes,  In's 

4     .... 

4^.... 
4M.... 
4^.... 

iH,.;. 

4^.... 
4^.... 
4%.... 
5     .... 
5H.... 
5M.... 
5^.... 

5H-... 

5^.... 
5M-... 
5H.... 
6     .... 
6H-... 
6M.  ... 

•Hi.--. 

6H-... 
65/g.... 
6%.... 
6^.... 
7     .... 

IH,  J. 

7%.... 

IHi.y. 

7^.... 

7^.... 
7^.... 

T»,.-;i 

8      

4.28 
4.42 
4.5G 
4.69 
4.8C 
4.97 
5.11 
5.24 
5.38 
5.52 
5.65 
5.79 
5.93 
6.07 
6.20 
6.34 
6.48 
6.61 
6.75 
6.89 
7.03 
7.16 
7.30 
7.44 
7.57 
7.71 
7.85 
7.99 
8.12 
8.26 
8.40 
8.53 
8.67 

3.75 
3.87 
3.99 
4.11 
4.23 
4.35 
4.47 
4.59 
4.71 
4.83 
4.95 
5.07 
5.19 
5.31 
5.43 
5.55 
5.67 
5.79 
5.91 
6.03 
6.15 
6.27 
6.39 
6.51 
6.63 
6.75 
6.87 
6.99 
7.11 
7.23 
7.35 
7.47 
7.58 

3.26 
3.37 
3.47 
3.58 
3.68 
3.78 
3.89 
3.99 
4.09 
4.20 
4.30 
4.41 
4.51 
4.61 
4.72 
4.82 
4.93 
5.03 
5.13 
5.24 
5.34 
5.45 
5.55 
5.65 
5.76 
5.86 
5.96 
6.07 
6.17 
6.28 
6.38 
6.48 
6.59 

2.95 
3.05 
3.14 
3.23 
3.33 
3.42 
3.52 
3.61 
3.70 
3.79 
3.89 
3.98 
.08 
.17 
.26 
.36 
.45 
.54 
.64 
.  73 

.8,: 

.92 
5.01 
5.11 
5.2, 
5.29 
5.39 
5.48 
5.58 
5.67 
5.76 
5.8G 
5.95 

2.6; 

2.72 
2.81 
2.89 
2.97 
3.  06 
3.14 
3.22 
3.31 
3.39 
3.48 
3.56 
3.  64 
3.73 
3.81 
3.89 
3.98 
.06 
.15 
.2C 
.31 
.40 
.48 
4.56 
4.6. 

2.23 
2.30 
2.38 
2.45 
2.52 
2.59 
2.66 
2.73 
2.80 
2.87 
2.94 
3.01 
3.08 
3.15 
3.22 
3.29 
3.37 
3.44 
3.51 
3.58 
3.65 
3.72 
3.79 
3.86 
3.93 

1.92 
1.98 
2.04 
2.10 
2.16 
2.22 
2.28 
2.34 
2.40 
2.46 
2.52 
2.58 
2.65 
2.71 
2.77 
2.83 
2.89 

1.601 
1.651 
1.702 
1.752 
1.803 
1.853 
1.904 
1.954 
2".  005 
2.055 
2.106 
2.156 
2.207 
2.257 
2.308 
2.358 
2.409 

1.466 
1.512 
1.558 
1.604 
1.650 
1.697 
1.743 
1.789 
1.835 
1.881 
1.928 
1.974 
2.02 

.284 
.324 
.364 
.405 
.445 
.486 
.526 
.566 
1.607 

1.147 
1.183 
1.219 
1.255 
1.291 

1.010 







To  determine  weight    per  foot  of  a  tube  of  a  given  Inside  Diameter, 

add  to  weights  in  above  list  the  weights  given  below  under 

corresponding  gauge  numbers. 


GAUGE  NO. 

13 

14 

15 

16 

11 

18 

19 

20      I    21      1   22 

23 

24 

Increase  in 
Lbs.per  Foot 

.2084 

.1590 

.1197 

.0975 

.0777 

.  0554 

.0407 

.02831   02361.0181 

.0144 

.0112 

AND    CONDENSERS    FOR    EVERV 


221 


Table  Showing  Weight  Per  Foot  of  Seamless 
Brass  Tubes 

American  or  B.  &  S.  Gauge,  Measured  in  Outside  Diameters 


GAUGE  NO. 

2 

3 

4 

5 

6 

7 

8 

9 

10 

11 

12 

13 

Thickness   of 
each    No.  in 

8 

CM 

jH 

as 

CM 

CO 

•**< 

CO 

g 

CM 
t- 

1 

1 

decimal  parts 

g 

i 

O 
* 

GO 

to 

^* 

1 

^H 

g 

§ 

GO 

K. 

of  inch 

CM 

CM 

H 

'"j 

"J 

"1 

0 

°. 

0 

Fr&c.  of  inch 

correspondi'g 
closely  to 

i 

M 

if 

ft 

ft 

& 

i 

ft 

WS 

<& 



Gauge   Nos.: 

Diameter 

Tubes,  In's 

i 

A 

i 

174 

.  167 

.  16 

15 

.25 

.23 

.22 

.20 

i 

.  38 

.  36 

.34 

.32 

.30 

.27 

.25 

A 

.49 

.46 

.43 

.39 

.36 

.33 

.31 

i.... 



.67 

.63 

.59 

.55 

.51 

.47 

.43 

.39 

.36 

9 

.80 

.75 

.70 

.64 

.59 

.54 

.49 

.45 

.41 

i.... 

1.09 

1.05 

.99 

.93 

.87 

.80 

.74 

.67 

.61 

.56 

.51 

.46 

^  

1.28 

1.21 

1.14 

1.06 

.98 

.90 

.83 

.76 

.69 

.63 

.57 

.51 

3 

1  46 

1  38 

1  29 

1  19 

1  10 

1  01 

92 

84 

76 

.69 

62 

56 

«.   •   •   • 

1.65 

1.55 

1.43 

1.32 

1.22 

.11 

1.01 

.92 

.83 

.75 

.68 

.61 

2  .  .   .   . 

1.84 

1.71 

1.58 

1.45 

1.33 

.22 

1.11 

1.00 

.91 

.82 

.74 

.67 

if  

2.02 

1.87 

1.73 

1.59 

1.45 

.32 

1.20 

1.09 

.98 

.89 

.80 

.72 

1  

2.21 

2.04 

1.88 

1.71 

1.57 

.42 

1.29 

1.17 

1.06 

.95 

.86 

.77 

\y%  

2.58 

2.37 

2.17 

1.98 

1,80 

.63 

1.48 

1.33 

1.20 

1.08 

.97 

.87 

l^t  

2.95 

2.70 

2.47 

2.24 

2.03 

.84 

1.66 

1.50 

1.35 

1.21 

1.09 

.98 

Iff... 

3.32 

3.03 

2.76 

2.50 

2.27 

2.05 

1.85 

1.66 

1.50 

1.34 

1.21 

1.08 

l^  

3.69 

3.36 

3.05 

2.77 

2.50 

2.26 

2.03 

1.83 

1.64 

1.47 

1.32 

1.19 

l«j^  

4.07 

3.69 

3.35 

3.03 

2.74 

2.46 

2.22 

1.99 

1.79 

1.61 

1.44 

1.29 

1%.... 

4.44 

4.03 

3.64 

3.29 

2.97 

2.6? 

2.40 

2.16 

1.94 

1.74 

1.56 

1.39 

1%.  ... 

4.81 

4.36 

3.94 

3.55 

3.20 

2.88 

2.59 

2.33 

2.08 

1.87 

1.67 

1.50 

2     .... 

5.18 

4.69 

4.23 

3.82 

3.44 

3.09 

2.77 

2.49 

2.23 

2.00 

1.79 

1.60 

2^  

5.55 

5.02 

4.53 

4.08 

3.G7 

3.30 

2.96 

2.6G 

2.38 

2.13 

1.91 

1.71 

2M  

5.92 

5.35 

4.82 

4.34 

3.9f 

3.51 

3.15 

2.82 

2.53 

2.26 

2.02 

1.81 

8H  ... 

6.30 

5.68 

5.12 

4.60 

4.14 

3.71 

3.33 

2.99 

2.67 

2.39 

2.14 

1.91 

2J^.  .  .  . 

6.67 

6.01 

5.41 

4.87 

4.37 

3.92 

3.52 

3.15 

2.82 

2.52 

2.26 

2.02 

2^.... 

7.04 

6.34 

5.71 

5.13 

4.61 

4.13 

3.70 

3.32 

2.97 

2.65 

2.37 

2.12 

Hi.... 

7.41 

6.67 

6.00 

5.39 

4.84 

4.34 

3.89 

3.48 

3.11 

2.78 

2.49 

2.22 

27-^.  .  .  . 

7.78 

7.00 

6.30 

5.65 

5.07 

4.55 

4.07 

3.65 

3.26 

2.91 

2.(J1 

2.33 

3     .... 

8.16 

7.34 

6.59 

5.92 

5.31 

4.75 

4.26 

3.81 

3.41 

3.05 

2.72 

2.43 

IK.... 

8.53 

7.67 

6.89 

6.18 

5.54 

4.96 

4.44 

3.98 

3.55 

3.18 

2.84 

2.54 

3M  

8.90 

8.00 

7.18 

6.44 

5.77 

5.17 

4.63 

4.14 

3.  70 

3.31 

2.96 

2.64 

3iMs  

9.27 

8.33 

7.48 

6.70 

6.01 

5.38 

4.81 

4.31 

3.85 

3.44 

3.07 

2.74 

3H-  •  •  • 

9.64 

8.66 

7.77 

6.97 

6.24 

5.59 

5.00 

4.47 

4.00 

3.57 

3.19 

2.85 

if*:..-. 

10.01 

8.99 

8.07 

7.23 

6.48 

5.79 

5.18 

4.64 

4.14 

3.70 

3.31 

2.95 

3%.  .  .  . 

10.39 

9.32 

8.36 

7.49 

6.71 

6.00 

5.37 

4.80 

4.29 

3.83 

3.42 

3.06 

3K... 

10.76 

9.65 

8.65 

7..  75 

6.94 

6.21 

5.55 

4.97 

4.44 

3.96 

3.54 

3.16 

To  determine  weight  per  foot  of  a  tube  of  a  given  Inside  Diameter, 

add  to  weights  in  above  list  the  weights  given  below  under 

corresponding  gauge  numbers. 


GAUGE  NO. 

2 

3 

4 

5 

6 

7 

8 

9 

10 

11 

12 

13 

Increase  in 
Ibs.  per  foot: 

1.532 

1.213 

.  9637 

.7642 

.6061 

.4806 

.3811 

.  3023 

.2397 

.1901 

.1507 

.1195 

j PUMPty  6" 

•  ••••••»»aw»w»u»»  fm  » 


222 


Table  Showing  Weight  per  Foot  of  Seamless 
Brass  Tubes 

(Continued) 

American  or  B.  &  S.  Gauge,  Measured  in  Outside  Diameters 


GAUGE  NO. 

14 

15 

16 

17 

18 

19 

20 

21 

22 

23 

24 

25 

26 

Thickness   of 
each    No.   in 

g 

1 

g 

~¥~ 

1 

1 

| 

1 

t- 

t— 

j» 

^iT 

decimal  paits 

3 

* 

K 

§ 

^ 

H 

co 

i! 

eS 

9 

SJ 

* 

S 

° 

g 

1-1 

of  inch: 

o 

°. 

°. 

. 

• 

<=>- 

_j 

. 

Frac.  of  inch 

correspondi't, 

i 

3 

1_ 

i 

closely  to 

16 

64 

32 

®4 

Gauge  Nos. 

Diameter 

Tubes,  In's 

A.... 

.045 

.04 

.041 

.039 

.037 

.034 

.032 

.028 

.027 

.024 

.022 

.020 

ft:;;: 

.090 

.086 

.08 

.07 

.068 

.062 

.057 

.053 

.041 

.043 

.038 

.035 

.032 

j.... 

.14 

.13 

.12 

.11 

.097 

.088 

.080 

.073 

.065 

.059 

.053 

.048 

.043 

&.  ... 

.18 

.17 

.15 

.14 

.13 

.114 

.104 

.094 

.084 

.076 

.067 

.061 

.054 

3. 

23 

21 

19 

.17 

.15 

.14 

.126 

.114 

.102 

.092 

.082 

.074 

066 

A 

.28 

.25 

.23 

.20 

.18 

.17 

.15 

.135 

.121 

.108 

.096 

.087 

.077 

*:;:: 

.32 

.29 

.26 

.24 

.21 

.19 

.17 

.155 

.139 

.124 

.111 

.100 

.089 

& 

37 

33 

30 

27 

24 

.22 

.20 

.176 

.156 

.141 

.125 

113 

.100 

.42 

.37 

.34 

.30 

.27 

.24 

.22 

.196 

.174 

.157 

.140 

.126 

.112 

»!!!:! 

.46 

.42 

.37 

.33 

.30 

.27 

.24 

.22 

.193 

.173 

.154 

.139 

.123 

4J 

.51 

.46 

.41 

.37 

.33 

.30 

.26 

.24 

.211 

.189 

.169 

.152 

.135 

**:;;.. 

.55 

.50 

.45 

.40 

.36 

.32 

.29 

.2^ 

.230 

.206 

.183 

.164 

.146 

§  .  .  .  . 

.60 

.54 

.48 

.43 

.39 

.35 

.31 

.28 

.248 

.222 

.198 

.177 

.158 

ft!  1  '.  '. 

.64 

.58 

.52 

.47 

.42 

.37 

.33 

.30 

.267 

.238 

.212 

.190 

.169 

i  — 

.69 

.62 

.'56 

.50 

.45 

.40 

.36 

.32 

.285 

.254 

.227 

-.203 

.181 

IK-  .  .  • 

.79 

.70 

.63 

.57 

.50 

.45 

.40 

.36 

.321 

.29*7 

.256 

.229 

IM.... 

.88 

.79 

.70 

.63 

.56 

.50 

.45 

.40 

.358 

.320 

.285 

.255 

liNi-  •  •  • 

.97 

.87 

.78 

.69 

.62 

.55 

.50 

.44 

.395 

.352 

.314 

.281 

\y^.  .  .  . 

1.06 

.95 

.85 

.76 

.68 

.61 

.54 

.48 

.43 

.384 

.343 

.317 

1%.  .  .  . 

1.16 

1.03 

.92 

.82 

.74 

.66 

.59 

.52 

.47 

.417 

.372 



1M-... 

1.25 

1.12 

1.00 

.89 

.79 

.71 

.63 

.56 

.50 

.450 

.401 

1%.... 

1.34 

1.20 

1.07 

.95 

.85 

.76 

.68 

.61 

.54 

.482 

.430 

2     

1.43 

1.28 

1.14 

1.02 

.91 

.81 

.73 

.65 

.58 

.514 

.459 

2  1/ 

1.53 

1.36 

1.22 

1  09 

97 

86 

77 

69 

.61 

.558 

-    2M^]] 

1.62 

1.44 

1.29 

1.16 

1.03 

.92 

.82 

.73 

.65 

.580 

2%.... 

1.71 

1.53 

1.36 

1.22 

1.08 

.97 

.86 

.77 

.69 

.612 

2H-  •  •  • 

1.80 

1.61 

1.44 

1.28 

1.14 

1.02 

.91 

.81 

.73 

.644 

2M-  •  •  • 

1.90 

1.69 

1.51 

1.35 

1.20 

1.07 

.96 

.85 

.76 

2%  

1.99 

1.77 

1.58 

1.41 

1.26 

1.12 

1.00 

.89 

.80 

2%.... 

2.08 

1.86 

1.66 

1.48 

1.32 

1.17 

1.05 

.93 

.83 

3     .... 

2.17 

1.94 

1.73 

1.54 

1.38 

1.23 

1.09 

.97 

.87 

2.27 

2.02 

1.80 

1.  62 

1.  43 

1.28 

.  14 

1.02 

.91 

3M- 

2.36 

2.10 

1.  88 

1.  68 

1.49 

1.  33 

.19 

1.  06 

.94 

33^ 

2.45 

2.19 

1.95 

1.  74 

.55 

1.  38 

.23 

1.  10 

.98 

v  /  8  •  •  •  - 

3^.... 

2.54 

2.27 

2.02 

1.80 

.61 

1.43 

.28 

1.14 

1.02 

•£...-, 

2.64 

2.35 

2.10 

1.87 

.67 

1.49 

.33 

.18 

1.05 

3M-... 

2.73 

2.43 

2.17 

1.93 

1.72 

1.54 

.37 

.22 

1.09 

3K.... 

2.82 

2.52 

2.24 

2.00 

1.78 

1.59 

.42 

.26 

1.13 

To  determine  weight  per  foot  of  a  tube  of  a  given  Inside  Diameter,  add 

to  weights  in  above  list  the  weights  given  below  in 

corresponding  gauge  numbers. 


GAUGE  NO. 

14 

15 

16 

17 

18 

19 

20 

21 

22 

23 

24 

25 

26 

Increase  in 
lb».   per   foot 

.0948 

.0752 

.0596 

.0473 

.0375 

.0297 

.0236 

.0187 

.0148 

.0117 

.009 

.0074 

.0059 

AND    CONDENSERS    FOR   EVERY  SERVICE 


223 


Table  Showing  Weight  Per  Foot    of    Seamless 
Brass  Tubes 

(Continued) 

American  or  B.  &  S.  Gauge,  Measured  in  Outside  Diameters 


GAUGE  NO. 

2 

CO 

1 

CM 

3 

4 

5 

S 

od 

6 

7 

gj 
••* 

8 
en 

i 

9 

CO 

10 

11 

M 

21 

Thickness  of  each  No.  in 
decimal  parts  of  inch 

CM 

I 

| 

Frac.  of  inch  correspond- 
ing closely  to  Gauge  No.: 

i 

44 

64 

if 

A 

g 

& 

* 

& 

A 

Diameter  Tubes. 
Inches 

4      
4H  
434    

11.13 
11.50 
11.87 
12.24 
12.62 
12.99 
13.36 
13.73 
14.10 
14.47 
14.85 
15.22 
15.59 
15.96 
16.33 
16.71 
17.08 
17.45 
17.82 
18.19 
18.56 
18.94 
19.31 
19.68 
20.05 
20.42 
20.79 
21.17 
21.54 
21.91 
22.28 
22.65 
23.03 

9.98 
10.31 
10.65 
10.98 
11.31 
11.64 
11.97 
12.30 
12.63 
12.96 
13.29 
13.62 
13.96 
14.29 
14.62 
14.95 
15.28 
15.61 
15.94 
16.27 
16.60 
16.93 
17.27 
17.60 
17.93 
18.26 
18.59 
18.92 
19.25 
19.58 
19.91 
20.24 
20  .  58 

8.95 
9.24 
9.54 
9.83 
10.13 
10.42 
10.72 
11.01 
11.31 
11.60 
11.90 
12.19 
12.49 
12.78 
13.08 
13.37 
13.67 
13.96 
14.26 
14.55 
14.84 
15.14 
15.43 
15.73 
16.02 
16.32 
16.61 
16.91 
17.20 
17.50 
17.79 
18.09 
18.38 

8.02 
8.28 
8.54 
8.80 
9.07 
9.33 
9.59 
9.85 
10.12 
10.38 
10.64 
10.90 
11.17 
11.43 
11.69 
11.95 
12.22 
12.48 
12.74 
13.  OC 
13.27 
13.  5o 
13.79 
14.05 
14.32 
14.58 
14.84 
15.10 
15.37 
15.63 
15.89 
16.15 
16.42 

7.18 
7.41 
7.64 
7.88 
8.11 
8.35 
8.58 
8.81 
9.05 
9.28 
9.51 
9.75 
9.98 
10.22 
10.45 
10.68 
10.92 
11.15 
11.38 
11.62 
11.85 
12.09 
12.32 
12.55 
12.79 
13.02 
13.25 
13.49 
13.72 
13.96 
14.19 
14.42 
14.66 

6.42 
6.63 
6.84 
7.04 
7.25 
7.46 
7.67 
7.88 
8.08 
8.29 
8.50 
8.71 
8.92 
9.12 
9.33 
9.54 
9.75 
9.96 
10.17 
10.37 
10.58 
10.79 
11.00 
11.21 
11.41 
11.62 
11.83 
12.04 
12.25 
12.45 
12.66 
12.87 
13.08 

5.74 
5.93 

6.11 
6.30 
6.48 
6.67 
6.85 
7.04 
7.22 
7.41 
7.59 
7.78 
7.97 
8.15 
8.34 
8.52 
8.71 
8.89 
9.08 
9.26 
9.45 
9.63 
9.82 
10.00 
10.19 
10.38 
10.56 
10.75 
10.93 
11.12 
11.30 
11.49 
11.67 

5.15 
5.30 
5.46 
5.63 
5.79 
5.96 
6.12 
6.29 
6.45 
6.62 
6.78 
6.95 
7.11 
7.28 
7.44 
7.61 
7.77 
7.94 
8.10 
8.27 
8.43 
8.60 
8.77 
8.93 
9.10 
9.26 
9.43 
9.59 
9.76 
9.92 
10.09 
10.25 
10.42 

4.58 
4.73 
4.88 
5.02 
5.17 
5.32 
5.47 
5.61 
5.76 
5.91 
6.05 
6.20 
6.35 
6.49 
6.64 
6.79 
6.94 
7.08 
7.23 
7.38 
7.52 
7.67 
7.82 
7.96 
8.11 
8.26 
8.41 
8.55 
8  70 
8.85 
8.99 
9.14 
9.29 

4.09 
4.22 
4.35 
4.49 
4.62 
4.75 
4.88 
5.01 
5.14 
5.27 
5.40 
5.53 
5.66 
5.79 
5.92 
6.06 
6.19 
6.32 
6.45 
6.58 
6.71 
6.84 
6.97 
7.10 
7.23 
7.36 
7.50 
7.63 
7.76 
7.89 
8.02 
8.15 
8.28 

43^   

43^  
45/6  
4^  

4^  

5     

5l/s  

5M  

5%  

51A  

55/8  

5M  
5H  
6 

61A  
6M  
6%  

6M 

6H  
6M  
6%  
7     
7M  
7M  

7ys  

7^ 

7^ 

7H  
7H  

8      

To  determine  weight  per  foot  of  a  tube  of  a  given  Inside  Diameter, 

add  to  weights  in  the  above  list  the  weights  given  below 

under  corresponding  gauge  numbers. 


GAUGE    NO. 

2 

3 

4 

5 

6 

7 

8 

9 

10         11 

Increase  in  Ibs.  per 
foot 

1  .  532 

1.213 

.9637 

.7642 

.6061 

.4806 

.3811 

.  3023 

.2397  .1901 

}r       PUMPING 

^ACHWfeRY,    AIR    COMPRESSORS      _f 

224 


Table  Showing  Weight  Per  Foot  of  Seamless 
Brass  Tubes 

(Continued] 

American  or  B.  &  S.  Gauge,  Measured  in  Outside  Diameters 


3AUGE  NO. 

Thickness   o] 
each    No.   in 
decimal  parts 
of  inch 

12 

13 

1 
S 

14 

15 

I 

16 

17 

1 

18 

1 

19 

20 

i 

21 

1 

22 
t~ 

23 

Frac.  of  inch 
correspond!  'g 

(IV 

TU 

ifr 

JW 

closely  to 
Gaug»  Nos. 
Diameter 
Tubes,  In  's 

4      .... 

4H-... 

4M 

3.66 
3.77 
3.89 

3.26 
3.37 
3  47 

2.91 
3.01 
3  10 

2.60 
2.68 
2.76 

2.32 
2.39 

2.46 

2.06 
2.14 
2.20 

1.84 
1.90 
1  96 

.64 
.69 

.74 

1.46 
1.51 
55 

.30 
.34 
39 

1.16 



t%.... 
4^.... 
48^ 

4.01 
4.12 
4.24 

3.58 
3.68 

3.78 

3.19 
3.28 
3  38 

2.84 
2.93 
3.01 

2.54 
2.61 
2.68 

2.26 
2.32 
2.39 

2.01 
2.07 
2  13 

.80 
.85 
.90 

.60 
.64 
69 

.43 
.47 



4M   • 

.36 

3  89 

3  47 

3.09 

2.76 

2  46 

2  19 

1.95 

74 

4J^.  • 

.47 

3.99 

3.56 

3.17 

2.83 

2.52 

2  25 

2.00 

79 

5     .  . 

.59 

4  09 

3.65 

3.26 

2.90 

2  59 

2  31 

2.05 

83 

5H 

4.71 

4.20 

3.75 

3.34 

2.98 

2  66 

2  36 

2.11 

5M  . 

4.82 

4  30 

3  84 

3.42 

3.05 

2  72 

2  42 

2  16 

5M-..- 
5K   • 

4.94 
5.06 

4.41 
4  51 

3.93 

4  02 

3.50 
3  59 

3.12 
3.20 

2.78 
2  85 

2.48 
2  54 

2.21 

2  26 



5%  • 

5.17 

4  61 

4  12 

3  67 

3  27 

2  91 

2  60 

5% 

5  29 

4  72 

4  21 

3  75 

3  34 

2  98 

2  65 

5H.... 

5.41 

4.82 

4.30 

3.83 

3.42 

3.04 

2.71 

6 

5  52 

4  93 

4  39 

3  92 

3  49 

3  11 

2  77 

6M 

5  64 

5  03 

4  49 

4  00 

3  57 

6^ 

5  76 

5  13 

4  58 

4  08 

3  64 

6% 

5  87 

5  24 

4  67 

4  16 

3  71 

6K 

5  99 

5  34 

4  76 

4  25 

3  78 

6^.... 
6% 

6.11 
6  22 

5.45 
5  55 

4.86 
4  95 

4.33 
4  41 

3.85 
3  93 



6^.... 

7 

6.34 
6  46 

5.65 
5  76 

5.04 
5  13 

4.49 
4  57 

4.01 
4  08 



7J-8    • 

6  57 

5  86 

5  23 

IX  • 

6  69 

5  96 

5  32 

7^8-  . 

6  80 

6  07 

5  41 

71^... 

6  92 

6  17 

5  50 

7%... 

7  04 

6  28 

5  60 

7  34  .  . 

7  15 

6  38 

5  69 

1%  

7  27 

6  48 

5   78 

8      .... 

7.39 

6.59 

5.87 



To  determine  weight  per  foot  of  a  tube  ot  a  given  Inside  Diameter, 

add  to  weights  in  the  above  list  the  weights  given  below 

under  corresponding  gauge  numbers. 


GAUGE  NO. 

12 

13 

14 

15  , 

16 

17 

18 

19 

20 

21 

22 

<*3 

Increase  in 
lb..  per  foot: 

.1507 

.1195 

.0948 

.0752 

.0596 

.0473 

.0375 

.0297 

.  0236 

.0187 

.0148 

.0117 

AND    CONDENSERS    FOR   EVERV  SERVICE 


225 


UNION       STEAM       PUMP       COMPANY 


Hyperbolic  Logarithms 


No. 

Log. 

No. 

Log. 

No 

Log. 

No. 

Log. 

No. 

Log. 

No. 

Log. 

1.01 

.0099 

2.30 

.8329 

3.68 

1.3029 

5.06 

1.6214 

6.44 

1.8625 

7.82 

2.0567 

1.02 

.0198 

2.32 

.8416 

3.70 

1.3083 

5.08 

1.6253 

6.46 

1.8656 

7.84 

2.0592 

1.03 

.0296 

2.34 

.8502 

3.72 

1.3137 

5.10 

1.6292 

6.48 

1.8687 

7.86 

2.0618 

1.04 

.0392 

2.36 

.8587 

3.74 

1.3191 

5.12 

1.6332 

6.50 

1.8718 

7.88 

2.0643 

1.05 

.0488 

2.38 

.8671 

3.76 

1.3244 

5.14 

1.6371 

6.52- 

1.8749 

7.90 

2.0669 

1.06 

.0583 

2.40 

.8755 

3.78 

1.3297 

5.16 

1.64C9 

6.54 

K8779 

7.92 

2.0694 

1.07 

.0677 

2.42 

.8833 

3.80 

1.3350 

5.18 

1.6448 

6.56 

1.8810 

7.94 

2.0719 

1.08 

.0770 

2.44 

.8920 

3.82 

1.3403 

5.20 

1.6487 

6.58 

1.8840 

7.96 

2.0744 

1.09 

.0862 

2.46 

.9002 

3.84 

1.3455 

5.22 

1.6525 

6.60 

1.8871 

7.98 

2.0769 

1.10 

.0953 

2.48 

.9083 

3.86 

1.3507 

5.24 

1.6563 

6.62 

1.8901 

8.00 

2.  0794 

1.12 

.1133 

2.50 

9163 

3.88 

1.3558 

5.26 

1.6601 

6.64 

1.8931 

8.02 

2.0819 

1.14 

.1310 

2  52 

.9243 

3.93 

1.3610 

5.28 

1.8639 

6.66 

1.8961 

8.04 

2.0844 

1.16 

.1484 

2.54 

.9322 

3.92 

1.3661 

5.30 

1.6677 

6.68 

1.8991 

8.06 

2.0869 

1.18 

.1655 

2.56 

.9400 

3.94 

1.3712 

5.32 

1.6715 

6.70 

1.9021 

8.08 

2.0894 

1.20 

.1823 

2.58 

9478 

3.96 

1.3762 

5.34 

1.6752 

6.72 

1.9051 

8.10 

2.0919 

1.22 

.1988 

2.60 

.9555 

3.98 

1.3813 

5.36 

.6790 

6.74 

1.9081 

8.12 

2.C943 

1.24 

.2151 

2  62 

.9632 

4.00 

1.  3863 

5.38 

.6827 

6.76 

1.9110 

8.14 

2.0968 

1.26 

.2311 

2.64 

.9708 

4.02 

1.3913 

5.40 

.6864 

6.78 

1.9140 

8.16 

2.0992 

1.28 

.2469 

2.66 

.9783 

4.04 

1.3962 

5.42 

.6901 

6.80 

1.9169 

8.18 

2.1017 

1.30 

.2624 

2.68 

.9858 

4.06 

1.4012 

5.44 

.6938 

6.82 

1.9199 

8.20 

2.1041 

1.32 

.2776 

2.70 

9933 

4.08 

1.4061 

5.46 

.  6974 

6.84 

1.9228 

8.22 

2.1066 

1.34 

.2927 

2.72 

.0006 

4.10 

1.4110 

5.48 

.7011 

6.86 

1.9257 

8.24 

2.1090 

1.36 

.3075 

2.74 

.0080 

4.12 

1.4159 

5.50 

.7047 

6.88 

1.9286 

8.26 

2.1114 

1.38 

.3221 

2.76 

.0152 

4.14 

1.4207 

5.52 

.7084 

6.90 

1.9315 

8.28 

2.1138 

1.40 

.3365 

2.78 

.0225 

4.16 

1.4255 

5.  54 

.7120 

6.92 

1.9344 

8.30 

2.  1163 

1.42 

.3507 

2.80 

.0296 

4.18 

1.4303 

5.56 

.7156 

6.94 

1.9373 

8.32 

2.1187 

1.44 

.3646 

2  82 

.0367 

4.23 

1.4351 

5.58 

.7192 

6.96 

1.9402 

8.34 

2.1211 

1.46 

.3784 

2.84 

.0438 

4.22 

1.4398 

5.60 

.7228 

6.98 

1.9430 

8.36 

2.  1235 

1.48 

.3920 

2.86 

.0508 

4.24 

1.4446 

5.62 

.7263 

7.00 

1.9459 

8.38 

2.1258 

1.50 

.4055 

2.88 

.0578 

4.26 

1.4493 

5.64 

.7299 

7.02 

1.9488 

8.40 

2.1282 

1.52 

.4187 

2.90 

.0647 

4.28 

1.4540 

5.66 

.7334 

7.04 

1.9516 

8.42 

2.1306 

1.54 

.4318 

2.92 

.0716 

4.30 

1.4586 

5.68 

.7370 

7.06 

1.9544 

8.44 

2.  1330 

1.56 

.4447 

2.94 

.0784 

4.32 

1.4633 

5.70 

.7405 

7.08 

1.9573 

8.46 

2.1353 

1.58 

.4574 

2.96 

.0852 

4.34 

1.4679 

5.72 

.7440 

7.10 

1.9G01 

8.48 

2.1377 

1.60 

.4700 

2.98 

.0919 

4.36 

1.4725 

5.74 

1.7475 

7.12 

1.9629 

8.50 

2.1401 

1.62 

.4824 

3.00 

.0986 

4.38 

1.4770 

5.76 

1.7509 

7.14 

1.9657 

8.54 

2.  1448 

1.64 

.4947 

3.02 

.1053 

4.40 

1.4816 

5.78 

1.7544 

7-16 

1.9685 

8.58 

2.1494 

1.66 

.5068 

3.04 

.1119 

4.42 

i:4861 

5.80 

1.7579 

7.18 

1.9713 

8.62 

2.1541 

1.68 

.5188 

3.06 

.1184 

4.44 

1.4907 

5.82 

1.7613 

7.20 

1.9741 

8.66 

2.1587 

1.70 

.5306 

3.08 

.1249 

4.46 

1.4951 

5.84 

1.7647 

7.22 

1.9769 

8.70 

2.1633 

1.72 

.5423 

3.10 

.1314 

4.48 

1.4996 

5.86 

1  7681 

7  24 

1.9796 

8.74 

2.  1679 

1.74 

.5539 

3.12 

.1378 

4.50 

1.5041 

5.88 

1.7716 

7.  '26 

1.9824 

8.78 

2.1725 

1.76 

.5653 

3.14 

.1442 

4.52 

1.5085 

5.90 

1.7750 

7.28 

1.9851 

8.82 

2.1770 

1.78 

.5766 

3.16 

.1506 

4.54 

1.5129 

5.92 

1.7783 

7.30 

1.9879 

8.86 

2.1815 

1.80 

.5878 

3.18 

1.1569 

4  56 

1.5173 

5.94 

1.7817 

7.32 

1.9906 

8.90 

2.  1861 

1.82 

.5988 

3.20 

1  1632 

4.58 

1.5217 

5.96 

1.7851 

7.34 

1.9933 

8.94 

2.1905 

1.84 

.6098 

3.22 

1.1694 

4.60 

1.5261 

5.98 

1.7884 

7.36 

1.9961 

8.98 

2.1950 

1.86 

.6206 

3.24 

1.1756 

4.62 

1.5304 

6.00 

1.7918 

7.38 

1.9988 

9.00 

2.1972 

1.88 

.6313 

3.26 

1.1817 

4.64 

1.5347 

6.02 

1.7951 

7.40 

2.0015 

9.04 

2.2017 

1.90 

.6419 

3.28 

1.1878 

4.66 

1.5390 

6.04 

1.7984 

7.42 

2.0041 

9.08 

2.2061 

1.92 

.6523 

3.30 

1.1939 

4.68 

1.5433 

6.06 

1.8017 

7.44 

2.  0069 

9.12 

2.2105 

1  94 

.6627 

3.32 

1.1999 

4.70 

1.5476 

6.08 

1.8050 

7.46 

2.0096 

9.16 

2.2148 

1.96 

.6729 

3.34 

1.2060 

4.72 

1  .  5518 

6.10 

1.8083 

7.48 

2.0122 

9.20 

2.  2192 

1.98 

.6831 

3.  36 

1.2119 

4.74 

1.5560 

6.12 

.8116 

7.50 

2.0149 

9.30 

2.  2230 

2.00 

.6931 

3.38 

1.2179 

4.76 

1.5602 

6.14 

.8148 

7.52 

2.0176 

9.50 

2.2513 

2.02 

.7031 

3.40 

1.2238 

4.78 

1.5644 

6.16 

.8181 

7.54 

2.0202 

9.70 

2.2721 

2  04 

.7129 

3.42 

1.2296 

4.80 

1.5686 

6.18 

.8213 

7.56 

2.0229 

9.90 

2.  2925 

2.06 

.7227 

3.44 

1.2355 

4.82 

1.5728 

6.20 

.8245 

7.58 

2.0255 

10.00 

2.3026 

2.08 

.7324 

3.46 

1.2413 

4.84 

1.5769 

6.22 

.8278 

7.60 

2.0281 

10.25 

2.3?79 

2.10 

.7419 

3.48 

1.2470 

4.86 

1.5810 

6.24 

.8310 

7.62 

2.0308 

10.50 

2.3513 

2  12 

.7514 

3.50 

1.2528 

4.88 

1.5851 

6.26 

.8342 

7.64 

2.0334 

10.75 

2.  3749 

2.14 

.7608 

3.52 

1.2585 

4.93 

1.5892 

6.28 

.8374 

7.66 

2.0360 

11.00 

2.3979 

2.16 

.7701 

3.54 

1.2641 

4.92 

1.5933 

6.30 

.8405 

7.68 

2.0386 

11.25 

2.4201 

2.18 

.7793 

3.56 

1.2698 

4.94 

1.5974 

6.32 

.8437 

7.70 

2.0412 

11.50 

2.4430 

2.20 

.7885 

3.58 

1.2754 

4.9fi 

1.6014 

6.34 

.8469 

7.72 

2.0438 

11.75 

2.4636 

2.22 

.7975 

3.60. 

1.2809 

4.98 

1.6054 

6.38 

.8500 

7.74 

2.0464 

12.00 

2.4849 

2.24 

.8065 

3.62 

1.2865 

5.00 

1  .  (5094 

6.38 

.8532 

7.76 

2.0490 

12.50 

2.5262 

2.26 

.8154 

3.64 

1.2920 

5.04 

1.6134 

6.40 

.  8563 

7.78 

2.f516 

13.00 

2.  5649 

2.28 

.8242 

3.66 

1.2975 

5.04 

1.6174 

6.42 

.8594 

7.80 

2.0541 

14.00 

2.6391 

PUMP  ING    M  AC  H INE  RY.   AIR   COMP  R  E S  S  OR  S 

jngyErgJE^^infing^ 

226 


B  A 

TT 

I,F. 

C  RE 

EK. 

MI 

CH 

IG 

AN, 

U. 

S.  A.        1 

Information  Required    for   Surface  and  Jet  Con- 
denser Installation 

To  select  the  proper  jet  condenser  or  surface  condenser 
with  the  auxiliary  pumps,  it  is  necessary  to  know  the  conditions 
under  which  the  condenser  will  operate. 

The  most  necessary  information  is :  The  amount  of  steam 
to  be  condensed;  the  vacuum  it  is  desired  to  maintain;  the 
temperature  of  the  cooling  water. 

As  in  many  cases  the  purchaser  cannot  state  the  first  con- 
ditions definitely,  it  is  necessary  to  know  the  other  details, 
which  will  serve  to  give  a  good  idea  of  the  requirements  of  the 
plant. 

In  stating  the  vacuum  required,  remember  that  the  higher 
the  vacuum,  the  larger  and  more  expensive  the  condenser  and 
pumps  must  be.  With  any  condenser,  the  smaller  the  quantity 
of  steam  handled,  the  higher  will  be  the  vacuum  obtainable, 
other  conditions  being  equal.  Also,  the  cooler  the  condensing 
water  or  the  larger  the  quantity,  the  better  will  be  the  vacuum 
obtainable. 

Please  answer  the  following  questions  as. fully  as  possible, 
and  we  will  give  you  the  benefit  of  our  experience  in  selecting 
the  proper  size  condenser. 

1.  What  is  the  number  of  pounds  of  steam  to  be  condensed 
per  hour? 

(a)  At  ordinary  load. 

(b)  At  peak  load. 

2.  What  vacuum  is  to  be  maintained  ? 

(a)  At  ordinary  load. 

(b)  At  peak  load. 

3.  What  is  the  temperature  of  the  cooling  water? 

(a)  Under  ordinary  conditions. 

(b)  Under  extreme  summer  conditions. 

4.  Is  there  always  an  ample  supply  of  cooling  water  available. 

5.  Is  the  cooling  water  fresh,  salt,  clear  or  muddy? 

6.  What  is  the  source  of  the  cooling  water  ? 

7.  How  far  from  proposed  condenser  is  the  source  of  supply 
of  cooling  water  located  ? 


L 

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COM  P  ANY 

J 

8.  Scate  size  of  suction  line,  if  one  is  already  installed. 

9.  State  vertical  height  cooling  water  must  be  lifted  by 
suction. 

10.  How  high  above  pump  must  cooling  water  be  delivered, 
after  passing  through  condenser? 

11.  If  the  unit  to  operate    condensing  is  a   steam  engine, 
give  the  following  information : 

(a)  Horse  power  at  peak  load. 

(b)  Type  of  engine  (simple  or  compound). 

(c)  Diameter  of  cylinder  (or  cylinders  if  compound). 

(d)  Length  of  stroke. 

(e)  Revolutions  per  minute. 

(f)  Steam  pressure  at  throttle. 

(g)  Point  of  cut  off. 

(h)  Is  engine  operating  at  peak  load  under  conditions 

specified? 
(i)   Do  you  expect  to  increase  this  load  after  condenser  is 

installed  ? 

12.  If  the  unit  to  operate  condensing   is  a  steam   turbine, 
give  the  following  information : 

(a)  Kilowatt  rating  at  peak  load. 

(b)  Give  steam  consumption  per  kilowatt  hour  at  peak 
load,  if  possible. 


»^M  A C  H^N^r^^I^^O^P^E^O  RS__| 

228 


w*  J£ 


Electrical 
Data 


SECTION  FOUR 


3 

Electrical  Units 

Current  (I).  The  strength  of  current  is  the  rate  at  which 
the  electricity  will  flow  through  a  conductor,  and  is  analogous 
to  the  rate  of  flow  of  water  through  a  pipe  in  gallons  per  second. 
The  unit  strength  of  current  is  called  the  ampere. 

Quantity  of  electricity    (Q).     The   quantity  of  electricity 
that  passes  through  a  circuit  is  comparable  to  the  quantity  oi 
water  that  flows  through  a  pipe,  and  equals  the  product  of  the 
rate  of  flow,  and  the  time,  that  is 
Q=IT. 

If  I  is  one  ampere,  and  T  is  one  second,  Q  is  one  coulomb, 
which  is  the  unit  quantity  of  electricity.  If  10  amperes  flow 
through  a  wire,  then  in  30  seconds  10X30=300  coulombs  of 
electricity  will  pass. 

Electromotive  Force   (E.  M.  F.).     Electromotive  force,  or 
electrical  pressure  is  that  which  causes  electricity  to  flow  in  a 
closed  circuit.     The  unit  of  E.  M.  F.,  which  is  the  volt,  is  the 
electrical  pressure  which  will  cause  a  current  of  one  ampere  to 
flow  through  a  resistance  of  one  ohm. 
1  Kilovolt=1000  volts. 
1  Millivolt  =.001  volts. 

Resistance  (R).  All  substances  offer  a  resistance  to  the 
passage  of  electricity  through  them,  and  the  amount  of  resist- 
ance depends  on  the  substance,  and  its  shape.  The  resistance 
of  all  metals  increases  with  an  increase  in  temperature,  while  the 
resistance  of  carbon  and  insulating  materials,  and  electrolytic 
solutions  decreases  with  an  increase  in  their  temperature. 

The  unit  of  resistance  is  the  ohm.  A  conductor  has  a 
resistance  of  one  ohm,  when  the  pressure  required  to  send  a 
current  of  one  ampere  through  it  is  one  volt. 

Ohm's  Law:  The  relation  between  current  (amperes), 
pressure  (volts),  and  resistance  (ohms),  is  stated  by  the  famous 
Ohm's  Law.  This  law  is  the  begining  of  our  scientific  knowledge 
of  electricity. 

The  law  is  stated  as  follows :  The  electric  current  along 
a  conductor  equals  the  pressure  divided  by  the  resistance. 

Pressure 
Current  =7: — T— 

Resistance. 

In  electric  units: 

Volts 

Amperes  =7^r~ 

.Ohms. 


MACHINERY;  AIR  COMPRESSORS 

JJ»lM.I>l>»»tllll»llUffl»<l*lll»lJgg^tt*B«a-?r»>»»^B^»t»««» 


230 


|1"   BATTLE 

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U. 

S. 

A. 

4 

Volts        =  Amperes  X  Ohms. 
Volts 


Ohms       =• 


Amperes. 

Power,  Watt,  Kilowatt:  The  flow  of  an  electric  current 
has  been  likened  to  the  flow  of  water  through  a  pipe.  A  current 
of  water  is  measured  by  the  number  of  gallons  or  pounds  flowing 
per  minute  ;  a  current  of  electricity  by  the  number  of  amperes, 
or  coulombs  per  second.  The  power  required  to  keep  -a  current 
of  water  flowing  is  the  product  of  the  current  in  pounds  per 
minute  by  head,  or  pressure,  in  feet. 

In  the  same  way,  the  power  required  to  keep  a  current  of 
electricity  flowing,  is  the  product  of  the  current  in  amperes  by 
the  resistance  in  volts.  This  gives  the  power  in  Watts.  One 
Watt  is  produced  when  a  current  of  one  ampere  flows  under  a 
pressure  of  one  volt. 

Volts  X  Amperes    =  Watts. 

Volts  X  Amperes. 

=  Kilowatts. 


Volts  X  Amperes 

-  -  -  =  Horse  Power. 
746 

1  Myriwatt  =10  Kilowatts. 

Work.  Commercial  Units:  In  order  to  compute  the 
amount  of  work  done  by  a  given  engine,  it  is  necessary  to  know 
the  time  it  has  been  running,  and  the  power  it  has  been  supplying, 
that  is  its  rate  of  doing  the  work.  If  the  power  is  measured  in 
Horse  Power,  and  the  time  in  Hours,  the  work  done  is  measured 
in  Horse-Power-Hours,  and  is  the  product  of  the  Horse  Power 
by  the  Hours. 

Similarly,  if  the  power  is  measured  in  Kilowatts,  and  the 
time  in  hours,  the  work  done  is  measured  in  Kilowatt-Hours, 
and  is  the  product  of  the  Kilowatts  by  the  Hours. 

The  Horse-Power-Hour,  and  the  Kilowatt-Hour  are  the 
commercial  units  of  work. 

1  H.  P.  hour  =  .  746  K.  W.  hours. 
1  K.  W.  hour  -1.34  H.  P.  hours. 

Two  other  units  of  work  are  also  used  in  computing  problems  : 
The  mechanical  unit  is  the  Foot-Pound.  The  electrical  unit  is 
the  Watt-Second,  also  called  the  Joule. 


3 

231 


1  H.  P.  hour  =  1,980,000  ft.  Ibs. 
1  K.  W.  hour  =2,654,200  ft.  Ibs. 
1  Joule  =.74  ft.  Ibs. 

The  following  are  the  electrical  units  of  Work  and  Power 
in  general  use : 

Work  Units :     Watt-second  =  joule  =  volt  —coulomb. 
K.  W.  hour  =3,600,000  Watt-seconds. 

Power  Units:      Watt  =  joule     per     second  =  volt-ampere  = 
volt-coulomb  per  second. 

Kilowat  =  1000  Watts. 

Kilowatts 


Kilovolt-Ampere  (A.  C.  unit)  = 


Power  factor. 


Power  Factor 

In  an  alternating  current  circuit,  it  is  customary  to  refer 
to  the  product  of  the  effective  volts  and  the  effective  amperes 
by  the  name  of  Apparent  Power,  and  to  measure  it  in  volt- 
amperes.  The  term  "cos  0"  is  then  called  the  Power  Factor. 
Thus  when  we  wish  to  compute  the  true  or  effective  power,  we 
find  the  apparent  power  (volts  x  amperes),  and  multiply  it  by 
the  Power  Factor  (cos  pf).  When  the  voltage  and  current  are 
in  phase,  the  term  (cos  <fi)  is  unity  (1)  and  the  "circuit  is  said  to 
have  unity  Power  Factor. 

The  Power  Factor,  then,  really  indicates  what  fraction  the 
true  or  effective  power  is  of  the  apparent  watts,  or  volt-amperes. 
It  is  generally  defined  by  the  equation 

_,  effective  power  watts 

Power  Factor  = — 

apparent  power     volts  x  amperes. 

Since  the  wattmeter  always  reads  the  effective  power,  we 
have  only  to  attach  a  wattmeter,  an  ammeter,  and  a  voltmeter 
to  a  circuit  to  find  the  Power  Factor,  and  from  it  the  phase 
difference  between  the  current  and  the  voltage.  The  product 
of  the  volts  and  the  amperes  gives  the  apparent  power  by  which 
the  wattmeter  reading  is  divided  to  give  the  Power  Factor. 


232 


c 

B  ATTLE 

C  REEK. 

MICHIGAN, 

U. 

S.A.        1 

Electrical  Equivalents 


One 
Watt 


One 
Kilowatt 


One 
Horse- 
Power 


A  RATE  of  doing  work. 

1 .  ampere  at  one  volt. 

.7373     foot-pounds  per  second 
44 . 238       foot-pounds  per  minute 
2654.28         foot-pounds  per  hour. 
.  5027     mile  pounds  per  hour. 
.00134  Horse-Power. 
7£T         Horse-Power. 

A  RATE  of  doing  work. 

737 . 3     foot-pounds  per  second. 
44238 .        foot-pounds  per  minute. 

502 . 7     mile-pounds  per  hour. 
1.34  Horse-Power. 

1A  RATE  of  doing  work. 
550.  foot-pounds  per  second 

33000.  foot-pounds  per  minute. 

375.  mile-pounds  per  hour. 

746.  watts. 

.  746     kilowatt. 


f  A  QUANTITY  of  work. 
One  I  2654.28         foot-pounds. 

Watt-         j  .503       mile-pounds. 

Hour  1.  ampere  hourXone  vc 

{  .00134  Horse-Power-Hour. 

f  A  QUANTITY  of  work. 
One  i  1,980,000.          foot-pounds. 

Horse-        1  375.          mile-pounds.  • 

Power  746 .         watt-hour. 

Hour  L  .746  kilowatt-hour. 

(  A  QUANTITY  of  current. 
One  1  One  ampere  flowing  for  one  hour 

Ampere       )      irrespective  of  the  voltage. 
Hour  [  Watt-hour  --5-  volts. 

(  Force  moving  in  a  circle. 
Torque       <  A  force  of  one  pound  at  a  radius 
I      of  one  foot. 


Horse  Power  of  Motors 

To  find  the  actual  or  brake  horse  power  of  an  alternating 


current  motor: 


Volts  X  Amperes  X  Cos 


X  M 


746 


2 


M  =  Motor  efficiency. 
N  =  Number  of  phases. 
Cos  ^=The  power  factor  of  the  motor. 
To  find  the  actual  or  brake  horse  power  of  a  direct  current 
motor  : 

Volts  X  Amperes  X  Efficiency  of  motor. 


B.  H.  P.= 


746 


(27) 


Alternating  Current 


Alternating  current  is  a  current  consisting  of  equal  half 
waves  in  successively  opposite  directions ;  it  flows  back  and  forth 
in  a  circuit  with  as  great  a  regularity  as  a  piston  moves  to  and  fro 
in  a  cylinder  of  a  steam  engine,  but  with  a  much  greater  rapidity. 


Fig.  94. 

Alternating  currents  are  represented  by  curved  lines,  as 
in  figure  94,  that  indicate  successive  positive  values  of  the  cur- 
rent by  loops,  or  half  waves  a-b  above  the  horizontal  line,  and 
the  negative  values  by  loop  b-c  below  the  horizontal  line.  Dis- 


AND    CONDENSERS    FOR   EVERT  SERVICE 


233 


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tances  along  the  horizontal  line  represent  time,  the  points  a-b-o 
represent  instants  when  the  current  is  zero,  from  a  the  current 
increases  in  a  positive  direction  to  a  maximum  value,  falls  to 
zero  at  b,  increases  to  a  maximum  negative  value,  and  again 
decreases  to  zero  at  £,  thus  completing  a  cycle.  These  cycles 
are  continually  repeated,  usually  twenty- five  to  sixty  or  more 
times  per  second,  the  number  of  cycles  per  second  is  the  fre- 
quency of  the  current,  and  the  time  required  for  the  current 
to  complete  a  cycle  is  a  period.  An  alternation  is  a  half  cycle, 
and  is  represented  by  the  curves  between  a-b,  or  between  b-c. 
The  frequency  is  generally  expressed  as  the  number  of  alterna- 
tions per  minute,  which  equals  2x60  x  number  of  cycles  per  second. 

Direct  Current 

A  direct  current  is  a  current  that  flows  in  one  direction ; 
that  is,  the  current  never  reverses  though  it  may  change  in  value, 
or  pulsate. 

Alternating  Current  Motors 

Synchronous  Motors 

Synchronous  Motors  are  so  called  because  they  run  in 
synchronism  with  the  alternator  supplying  the  energy  to  drive 
them.  Such  motors  find  considerable  application  in  power- 
transmission  systems.  They  possess  the  disadvantage  that  they 
are  not  inherently  self-starting,  so  that  they  have  not  been  very 
generally  adapted  for  drdinary  power  requirements.  Their 
speed  is  constant,  regardless  of  load,  which  characteristic  is 
often  valuable.  A  characteristic  which  makes  them  more 
particularly  adapted  to  use  in  power-transmission  systems  is 
that  their  power  factor  may  be  controlled  and  varied  through 
a  wide  range  by  varying  the  field  excitation. 

Induction  Motors 

A  single  phase  motor  has  no  starting  torque,  and  this  neces- 
sitates that  the  motor  be  started,  either  as  a  polyphase  motor 
by  applying  polyphase  power  to  it,  or  that  it  be  provided  with 
auxiliary  windings  to  start  it  as  a  repulsion  motor.  All  of  these 
methods  are  used  in  practice,  but  the  single-phase  motor  is  gen- 
erally used  only  in  small  sizes. 

The  majority  of  motors  used  in  the  alternating  current,  are 
the  polyphase  type,  either  2  or  3  phase. 


PUMPING   MAC  HINE  R.Y-    AlR   COMPRESSORS      _J 

mgi  »  .....  •«,  .  fs^-^ffn  *  g»Vfg-«  *  .  .  »  .r^g^nawrgTnriri^^  j 


234 


U.  S.  A. 


Induction  motors  are  classified  as  squirrel  cage,  or  as  wound 
rotor  motors  according  to  the  type  of  rotor. 

In  squirrel  cage  motors,  the  inductors  are  copper  bars  em- 
bedded in  longitudinal  slots  in  the  laminated  steel  rotor  core, 
and  are  connected  in  parallel  to  short-circuiting  copper  rings, 
one  at  each  end  of  the  rotor. 

In  the  wound  rotor,  the  winding  is  polar,  and  the  terminals 
of  the  windings  are  connected  to  a  resistance  carried  on  the 
rotor  spider,  or  through  slip  rings  to  an  external  resistance, 
which  resistance  may  be  cut  out  when  the  proper  speed  is  at- 
tained. Wound  rotor  motors  are  also  called  slip  ring  motors. 
Polyphase  squirrel  cage  motors  are  used  for  constant  speed 
service  where  starting  and  reversing  are  infrequent.  Their 
starting  torque  is  relatively  small,  and  a  large  starting  current 
(2  to  6  times  the  full  load  current)  is  drawn  from  the  line,  if  the 
motor  must  start  full  load  torque. 

Squirrel  cage  motors  are  adapted  to  driving  centrifugal 
pumps,  generator  sets,  blowers  and  any  other  machinery  where 
a  small  starting  torque  is  required. 

Slip  ring  or  wound  rotor  motors  give  about  IX  times  the 
full  load  torque  with  approximately  IX  times  full-load  current, 
making  them  suitable  for  use  where  a  minimum  starting  current 
is  desirable. 

Slip  ring  or  wound  rotor  motors  are  adapted  to  that  class 
of  service  which  requires  a  heavy  starting  torque,  such  as  driving 
power  reciprocating  pumps,  air  compressors  or  other  machinery 
which  have  to  start  against  a  full  load. 

The  synchronous  or  no  load  speed  of  any  induction  motor 
can  be  computed  from  the  equation. 

60  XF  (46 

nr~ 

S=  Speed  in  R.  P.  M. 
F  =  Frequency  in  cycles  per  second. 
P  =  Pairs  of  poles. 
Example 

What  is  the  speed  of  a  4  pole  60  cycle  motor? 

60X60 
S  =  -      —  =  1800  R.  P.M. 


L .  .4?j?.  .ggNpE*y^ 


235 


I- 

u 

N 

I  O 

N 

STEAM 

P 

U 

M 

P 

C  O 

M  P  ANY     n§ 

The  actual  or  full  load  speed  is  less  than  the  synchronous 
or  no  load  speed  owing  to  the  losses  in  the  rotor.  The  difference 
between  the  full  load  and  the  no  load  speed  is  called  the  slip, 
see  tables  on  pages  236-237. 


Speed  of  Rotary  Field  For  Different  Numbers 
of  Poles  and  For  Various  Frequencies 


Speed  of  Revolving  Magnetism,  in  Revolutions  per  minute,  when 


SS 

.Frequency  is: 

I* 

fc  0 

25 

30 

33M 

40 

50 

60 

66% 

80 

100 

120 

125 

133^ 

2 

1500 

1870 

2000 

2400 

3000 

3600 

4000 

4800 

6000 

7200 

7500 

8000 

4 

750 

900 

1000 

1200 

1500 

1800 

2000 

2400 

3000 

3600 

3750 

4000 

6 

500 

600 

667 

800 

1000 

1200 

1333 

1600 

2000 

2400 

2500 

2667 

8 

375 

450 

500 

600 

750 

900 

1000 

1200 

1500 

1800 

1875 

2000 

10 

302 

360 

400 

480 

600 

720 

800 

960 

1200 

1440 

1500 

1600 

12 

250 

300 

333 

400 

500 

600 

667 

800 

1000 

1200 

1250 

1333 

14 

214 

257 

286 

343 

428 

514 

571 

686 

857 

1029 

1071 

1143 

16 

188 

225 

250 

300 

375 

450 

500 

600 

750 

900 

938 

1000 

18 

167 

200 

222 

267 

333 

400 

444 

533 

667 

800 

833 

889 

20 

150 

180 

200 

240 

300 

360 

400 

480 

600 

720 

750 

800 

22 

136 

164 

182 

217 

273 

327 

364 

436 

545 

655 

682 

720 

24 

125 

150 

167 

200 

250 

300 

333 

400 

500 

600 

625 

667 

Slip  of  Induction  Motors 


ft 

Slip  at  full  load  per  cent 

Capacity  of 

Slip  at  full  load  per  cent 

fe^ 

ett^^j 
O  offi 

Usual  limits 

Average 

Motor,  H.  P. 

Usual  limits 

Av'age 

y% 

20-40 

30 

15 

5-11 

8 

1A 

10-30 

20 

20 

4-10 

7 

1A 

10-20 

15 

30 

3-9 

6 

8-20 

14 

50 

2-8 

5 

2 

8-18 

13 

75 

1-7 

4 

3 

8-16 

12 

100 

1-6 

3.5 

5 

7-15 

11 

150 

1-5 

3 

71A 

6-14 

10 

200 

1-4 

2.5 

10 

6-12 

9 

300 

1-3 

2 

236 


R 

ATTL 

E 

c 

R 

E 

E 

K. 

M 

ICHIGAN,      U.  S.  A^Jj 

Full  Load  Speed  of  Induction  Motors 


Full  load  speeds  of  alternating  current  motors  based  on  4%  slip 


ja 

• 

•go 

Cycles 

3 

£"0 

25 

27 

30 

33H 

40 

42 

50 

60 

100 

2 

1440 

1560 

1730 

1920 

2300 

2420 

2880 

4 

720 

780 

865 

960 

1150 

1210 

1440 

1725 

2880 

6 

480 

520 

575 

640 

770 

807 

960 

1150 

1920 

8 

360 

390 

433 

480 

575 

605 

720 

862 

1440 

10 

290 

310 

345 

385 

460 

485 

575 

690 

1150 

12 

240 

260 

288 

320 

385 

403 

480 

575 

960 

14 

205 

222 

247 

275 

330 

346 

412 

492 

822 

16 

180 

195 

216 

240 

287 

302 

360 

431 

720 

18 

160 

171 

192 

214 

256 

268 

320 

384 

640 

20 

142 

156 

173 

192 

230 

242 

287 

345 

575 

Induction  Motors 
220-440-2200  Volts 


Synch- 
ronous 
o         ^ 

Approxi- 
mate 
Full  Load 

Efficiency 
Per  Cent 

Power  Factor 
Per  Cent 

v. 

opeed 

Speed 

1 

O    K 

PH   O 

%  0 

o 

u 

-9   05 

w 

M 
o 

3 

tfl 

*y 

1 

jj 

1 

1 

1 

1 

•n 
1 

rt 

1 

5  j§ 

0 

CJ 

U 

0 

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j_J 

«—  i 

P 

p 

,—4 

o^ 

12 

o 

* 

o 

X 

* 

1 

* 

K 

* 

I 

5 

1 

4 

750 

1800 

690 

1700 

74 

77 

77 

76 

60 

72 

80 

83 

2 

6 

500 

1200 

460 

1120 

82 

84 

84 

86 

60 

72 

78 

80 

5 

6 

500 

1200 

460 

1120 

84 

86 

86 

85 

78 

84 

86 

87 

10 

6 

500 

1200 

465 

1135 

85 

86 

86 

84 

80 

86 

89 

90 

20 

6 

500 

1200 

470 

1135 

87 

88 

87^ 

87 

82 

89 

91 

90 

50 

8 

375 

900 

360 

850 

87 

88 

88 

88 

78 

86 

89 

9fr 

100 

10 

300 

720 

288 

690 

89 

90 

90 

90 

83 

89 

91 

91 

200 

12 

.... 

600 

.... 

575 

91 

92  H 

92 

91 

85 

91 

92 

91 

Note:     2200  volt  motors  are  seldom  made  in  sizes  under  20  Horse  Power. 


AND    CONDENSERS    FOR    E VERV  SERVICE 


UNION       STEAM       PUMP       COM  P  ANY 


Ampere  Ratings  of  A.  C.  Motors 


Single  Phase 

Two  Phase 

Three  Phase 

Volts 

Volts 

Volts 

H  P 

110 

220 

440 

550 

110 

220 

440 

550 

2200 

110 

220 

440 

550 

200 

v% 

y. 

4  0 

?,  0 

1  0 

8 

.  ' 

Vi 

7  5 

3  75 

1  9 

1  5 

3  ? 

1  6 

8 

6 

3  6 

1  8 

9 

.7 

ZA 

10 

2  5 

2 

1 

12.5 

6.25 

3.2 

2.5 

6.2 

3.0 

1.6 

1.2 

7.2 

3.6 

1.8 

1.4 

iu 

18 

9 

4  5 

3  6 

2 

24 

12 

6 

4.8 

10. 

5.0 

2.5 

2.0 

1.6 

5.8 

2.9 

2.3 

3 

34 

17 

8.5 

6.8 

14.2 

7.0 

3.6 

2.8 

. 

6.4 

8.2 

4.1 

3.3 

. 

4 

43 

22 

11 

8.6 

19 

9.0 

5 

4 

22 

11 

6 

4.5 

.  .  . 

5 

55 

28 

14 

11 

24 

12 

6 

5 

28 

14 

7 

6 

7V* 

80 

40 

20 

16 

33 

17 

9 

t 

39 

19 

10 

8 

.  .  . 

10 

105 

53 

25 

21 

47 

23 

12 

10 

54 

27 

14 

11 

15 

145 

73 

36 

29 

70 

35 

18 

14 

81 

40 

20 

16 

20 

200 

100 

50 

40 

90 

45 

23 

18 

104 

52 

26 

21 

.  .  . 

25 

250 

125 

63 

50 

112 

56 

28 

23 

6 

130 

65 

33 

26 

7 

30 

295 

148 

74 

59 

132 

66 

33 

26 

7 

152 

76 

38 

30 

8 

40 

370 

185 

93 

74 

175 

88 

44 

35 

9 

202 

101 

51 

41 

10 

50 

216 

108 

54 

43 

11 

250 

125 

63 

50 

13 

60 

260 

130 

65 

5? 

13 

300 

150 

75 

60 

15 

75 

324 

16? 

81 

65 

16 

375 

187 

94 

75 

19 

100 

43? 

?16 

108 

8f> 

?? 

500 

?50 

1?5 

100 

25 

125 

540 

270 

135 

108 

27 

625 

312 

156 

125 

31 

150 

648 

3?^ 

16? 

1?1 

3? 

75< 

375 

18S 

15( 

37 

175 

758 

379 

189 

15? 

38 

875 

438 

?19 

175 

44 

200 

864 

432 

216 

173 

43 

1000 

500 

250 

?00 

49 

250 

1080 

540 

?70 

216 

54 

1250 

625 

313 

250 

63 

300 

1298 

649 

3?5 

259 

65 

1500 

750 

375 

300 

75 

400 

1730 

865 

433 

346 

87 

2000 

1000 

500 

400 

100 

500 



|2160 

1080 

540 

432|  108 

2500 

1250 

62a 

500 

125 

Direct  Current  Motors 

Direct  current  motors  are  classified  according  to  their  wind- 
ing into  series-wound,  shunt-wound  and  compound-wound. 

The  series-wound  motor  is  adaptable  to  variable  speed 
work,  such  as  elevator  service,  crane  service,  etc.,  on  account  of 
its  speed-torque  characteristics.  The  series-wound  motor  de- 
velops almost  any  torque  demanded  of  it,  but  with  a  reduction 
in  speed,  so  that  it  is  especially  adapted  to  hard  work  where 
constant  speed  is  not  essential. 


238 


The  shunt-wound  motor  is  used  almost  \miversally  for  con- 
stant speed  service,  for  it  maintains  approximately  constant  speed 
regardless  of  load.  The  shunt-wound  motor  has  a  rather  low 
starting  torque,  and  is  adapted  to  such  uses  as  driving  blowers, 
and  other  machinery  in  which  the  starting  torque  required  is 
small. 

The  compound-wound  motor  which  is  a  combination  of  the 
series-wound  and  shunt-wound  motors  has  an  advantage  of  a 
large  starting  torque,  and  is  particularly  adapted  to  driving 
power  reciprocating  pumps,  centrifugal  pumps,  air  compressors, 
and  other  machinery. 

Ampere  Ratings  of  D.  C.  Motors 


H.  P. 

Rating  of  D.  C.  Motors 

Ampere  Capacity  of  Fuses 
for  Motors 

Full  Load  Amperes 

115  Volts 

230  Volts 

500  Volts 

115  Volts 

230  Volts 

500  Volts 

H 

1.4 

.70 

.35 

5 

5 

5 

% 

1.8 

.90 

.46 

5 

5 

5 

H 

2.2 

1.1 

.54 

5 

5 

5 

1A 

4.3 

2.2 

1.0 

7 

5 

5 

% 

6.2 

3.1 

1.5 

10 

5 

5 

l 

8.0 

4.0 

1.9 

15 

7 

5 

2 

16 

8.0 

3.8 

25 

15 

7 

3 

24 

12 

5.5 

30 

20 

10 

4 

32 

16 

7.2 

50 

25 

10 

5 

38 

19 

9.0 

50 

30 

15 

7^ 

58 

29 

13 

80 

50 

20 

10 

75 

38 

17.5 

100 

50 

25 

12^ 

94 

47 

22 

125 

70 

30 

15 

112 

56 

26 

150 

70 

35 

20 

148 

74 

34 

200 

100 

50 

25 

185 

93 

43 

275 

125 

60 

30 

220 

110 

51 

275 

150 

70 

35 

255 

125 

60 

325 

175 

80 

40 

285 

145 

67 

400 

200 

90 

45 

320 

160 

75 

400 

200 

100 

60 

350 

175 

83 

450 

225 

125 

60 

420 

210 

99 

550 

275 

125 

75 

520 

260 

122 

800 

325 

175 

90 

625 

315 

145 

100 

700 

350 

160 

125 

875 

440 

200 

150 

1050 

525 

240 

175 

1225 

615 

280 

200 

1400 

700 

320 

239 


UNION       S  T  E"  AM       P  U  M  P       CO  M  P  ANY 


Selection  of  Motors  and  Controllers 

The  selection  of  the  proper  type  of  motor  and  controlling 
equipment  to  be  used  with  centrifugal  pumps,  air  compressors, 
power  pressure  pumps  and  power  vacuum  pumps  is  very  essential. 

While  the  local  conditions  may  govern  to  some  extent  the 
type  of  motor  and  controlling  equipment  to  use,  the  following 
paragraphs  give  the  customary  types  of  motors  and  controlling 
equipment  to  use  with  machinery,  such  as  we  manufacture. 

For  direct  current  motors,  we  recommend  the  compound- 
wound  type  for  driving  centrifugal  pumps,  air  compressors, 
power  pressure  pumps  and  power  vacuum  pumps. 

For  alternating  current  motors,  we  recommend  the  squirrel 
cage  type  for  driving  centrifugal  pumps,  and  the  wound-rotor 
or  slip-ring  type  motors  for  driving  power  pressure  pumps, 
power  vacuum  pumps  and  air  compressors. 

For  reciprocating  machinery  such  as  power  pressure 
pumps  and  power  vacuum  pumps,  which  are  to  operate  under 
automatic  control,  we  recommend  that  the  motor  be  a 
size  larger  than  is  regularly  required.  This  is  due  to  the  fact 
that  under  automatic  control,  the  machinery  has  to  start  up 
under  full  load,  which  requires  a  very  heavy  starting  torque. 

On  the  following  pages  is  illustrated  and  described  the  proper 
electrical  control  equipment  to  be  used  in  connection  with  cen- 
trifugal pumps,  power  pressure  pumps,  air  compressors  and  power 
vacuum  pumps.  The  electrical  control  equipment  as  given, 
covers  both  direct,  and  alternating  current  apparatus,  and  in- 
cludes the  manual  starters,  as  well  as  the  self  starters. 


Electrical  Control  Equipment 

(The  Cutler-Hammer  Mfg.  Co.) 

For  Centrifugal  Pumps,  Air  Compressors,  Power  Pressure 
Purrfps,  and  Power  Vacuum  Pumps 

Motors:     Direct  Current,  Compound  Wound 
Manual  Starters 

Standard  duty  motor  starters  with  low  voltage  protection, 
Bulletin  2111  up  to,  and  including,  35  HP-115  volts,  and  50 
HP-230  or  550  volts. 


240 


The  standard  duty  starter  consists  of  a  sliding  contact 
type  starting  panel,  with  armature  resistor  self-contained, 
mounted  on  a  wall  type  frame.  The  low  voltage  protection 
feature  stops  the  motor  when  the  voltage  drops  or  fails  alto- 
gether and  prevents  it  from  restarting  when  normal  voltage  is 
restored.  This  protects  both  the  machine  and  operator  against 
the  motor's  starting  unexpectedly. 


Bulletin  21 11. 


With  cover  removed, 
to  show  construction. 


Heavy  duty  manual  starters  with  low  voltage  protection, 
Bulletin  2131.  Sliding  contact  type,  similar  to  Bulletin  2111, 
except  greater  capacity  resistor,  up  to  and  including  20HP-115 
to  550  volts.  Larger  sizes,  up  to  and  including  125HP,  115 
volts  and  200HP-230  or  550  volts  are  of  the  multiple  switch 
type. 

The  multiple  switch  starter  consists  of  a  slate  front  con- 
taining a  number  of  levers  which,  when  closed  in  sequence, 
function  similarly  to  the  sliding  contact  type  starter.  The 
levers  are  so  interlocked,  that  they  can  only  be  closed  in  se- 
quence. All  starters  up  to  75HP.-115  volts  and  100HP,-230 
and  550  volts  are  in  wall  type  enclosing  cases.  Larger  sizes  are 
arranged  for  floor  mounting. 


Bulletin  2131,  with  cover 
removed. 


Bulletin  2131  Multiple  Switch  Type, 
with  cover  removed. 


-    - 


AND    C 


241 


D.  C.  Automatic  Motor  Starters 


Time  limit  type  automatic  starters,  Bulletin  6106,  up  to 
60HP-115  volts,  125HP-230  volts  and  200HP-550  volts.  They 
can  be  controlled  by  pushbutton  master  stations,  snap  switch, 
float  switch,  pressure  regulator,  and  other  accessories. 

The  accelerating  movement  consists  of  a  number  of  fingers 
which  cut  out  successive  steps  of  resistor.  This  movement 
is  controlled  by  an  oil  filled  dash  pot.  In  addition,  the  larger 
sizes  include  a  magnetic  main  line  contactor. 


Bulletin  6106. 

Alternating  Current 

Motors:     Single  Phase,  Repulsion  Type 
Manual  Starters 

Single  phase  motor  starters,  Bulletin  9111,  with  low-voltage 
protection,  up  to  and  including  20HP-110  volts  and  30HP-220 
volts. 

These  single  phase  motor  starters  are  similar  in  construc- 
tion to  the  Bulletin  2111,  but  are  arranged  for  alternating 
current  service.  They  consist  of  a  slate  panel  with  the  sliding 
contact  type  starting  mechanism  and  can  be  used  witli  either 
commutator  or  repulsion  type  single  phase  motors. 


Bulletin  91 11 


With  cover  removed. 


242 


CRE  E  K.     M  I C  H  I  G  AN , 


1 


Across-the-line  type  manual  starters,  Bulletin  9115,  with 
thermal  overload  cutouts,  up  to  and  including  1  HP-110  volts, 
3  HP-220  volts  and  5HP-440  or  550  volts— single  phase. 

These  starters  consist  of  a  3  pole  manually  operated  con- 
tactor with  two  thermal  overload  cutouts,  mounted  on  a  slate 
panel  in  an  enclosing  case.  The  operating  handle  and  locking 
levers  are  on  the  outside  of  the  case.  Contacts  are  of  new  roller 
type-double  contact.  For  single  phase  service  the  center  pole 
is  left  "dead." 


Bulletin  9115. 

A.  C.  Automatic  Motor  Starters 

Across-the-line  type  self-starters,  Bulletin  9586,  up  to 
15HP-110  volts,  30HP-220  volts  and  40HP-440  or  550  volts. 

These  starters  consist  of  a  positive  acting,  three  pole  mag- 
netic contactor  and  C-H  Thermal  Overload  Relays,  mounted 
on  a  panel  in  a  split  case.  For  single  phase  service,  the  center 
pole  is  left  "dead."  The  controller  is  operated  by  a  remote 
control  pushbutton  master  switch  or  by  any  type  of  single 
pole  switch  such  as  a  snap  switch,  pressure  regulator,  etc. 

The  C-H  Thermal  Overload  Relays  provide  ideal  protec- 
tion at  all  times. 


Bulletin  9586  Type  AAA 


Bulletin  9586  Types  AA  or  A. 


r 


243 


E3 

N 

I  O 

N 

STEAM 

P 

UM 

P 

C  O 

M 

PANY 

-4 

Primary  resistor  type  automatic  starters,  Bulletin  9605, 
up  to  and  including  15HP-220  volts,  and  30HP-440  or  550 
volts,  single  ohase. 

This  is  a  three  pole  starter,  providing  one  step  of  primary 
resistor  on  starting.  It  consists  of  two,  three-pole  contactors 
and  C-H  Thermal  Overload  Relays  mounted  on  a  slate  panel 
in  an  enclosing  case.  For  single  phase  service  the  center  pole 
is  left  "dead."  The  first  contactor  closes  the  circuit  with  re- 
sistance inserted  and  the  closing  of  the  second,  which  is  timed 
by  an  oil  dash-pot,  cuts  out  the  resistor,  connecting  the  motor 
directly  to  the  line.  The  overload  relays  protect  the  motor 
from  overload  at  all  times  and  when  tripped  can  be  reset  from 
the  outside  of  the  case. 


Bulletin  9605. 


Motors:    A.  C.   2  or  3  Phase  Squirrel  Cage 

Manual  Starters 

Across-the-line  type  manual  starters,  Bulletin  9115,  with 
thermal  overload  cutouts,  up  to  and  including  3  HP— 110  volts, 
5  HP-220  volts  and  7^  HP-440  or  550  volts— two  or  three 
phase. 

These  starters  consist  of  a  three  or  four  pole  manually 
operated  roller  type  contactor  and  two  thermal  overload  cut- 
outs, mounted  on  a  slate  panel  in  an  enclosing  case.  The 
four  pole  contactor  is  for  two  phase,  four  wire  service  only. 


A.CHINERY,    AIR   COMPR 


244 


Operating  and  locking  levers  are  on  outside  of  case.     Thermal 
overload  cutouts  provide  overload  protection  at  all  times. 


Bulletin  9115. 


Panel  type,  fused  starting  switches,  with  low-voltage 
protection,  Bulletin  9116,  up  to  and  including  3HP-110  volt 
and  5HP-220  to  550  volts. 

The  panel  type  fused  starter  consists  of  a  three-pole  fully 
enclosed  switch,  fused  and  so  designed  that  in  starting  the 
fuses  are  not  in  circuit,  but  when  in  the  running  position  the 
fuses  are  in  the  circuit  for  protecting  the  motor.  The  cover 
can  be  lowered,  for  renewing  fuses.  This  starter  also  provides 
low-voltage  protection. 


Bulletin  91 16. 


With  cover  removed 
to  show  construction. 


245 


Primary  resistor  type  manual  starters,  Bulletin  9118,  for 
motors  up  to  and  including  7J^HP-110  volts  and  10HP-220 
to  550  volts. 

This  starter  is  for  use  on  motors  that  cannot  be  thrown 
directly  across  the  line,  and  which  do  not  require  the  more 
costly  auto-transformer  starter  (compensator).  It  is  a  panel 
type  starter,  similar  to  Bulletin  9116,  except  that  it  provides 
one  step  of  resistance  in  each  phase  of  the  primary  circuit  when 
starting.  This  cuts  down  the  large  current  inrush  to  the  motor 
on  starting.  It  is  provided  with  running  fuses,  provides  low- 
voltage  protection  and  is  fully  enclosed,  being  operated  by  a 
lever  on  the  outside  of  the  case. 


Bulletin  9118. 

Auto-transformer  starters,  Bulletin  9141,  up  to  and  in- 
cluding 25HP-110  volts  and  125HP-220  to  2200  volts. 

This  type  of  starter  in  the  smaller  sizes  is  self-contained, 
consisting  of  a  metal  case  containing  two  auto-transformers, 
switching  mechanism,  overload  and  low-voltage  protection 
features.  The  switching  mechanism  which  operates  under  oil, 
functions  to  connect  the  starting  transformer  to  the  power 
lines,  also  connecting  the  motor  to  taps  on  the  transformers 
for  starting,  without  drawing  excessive  current  from  the  line. 
When  the  motor  is  approximately  up  to  speed,  operation  of 
the  lever  serves  to  disconnect  the  starting  transformers  and 
connects  the  motor  directly  to  the  line. 

The  low-voltage  protection  feature  can  be  operated  me- 
chanically at  the  starter  or  by  means  of  pushbuttons  at  a  re- 
mote point  when  it  is  desired  to  stop  the  motor.  The  overload 
release  feature  will  not  trip  on  small  momentary  overloads. 


246 


BATTLE       CREEK.     M  I C  H  I  G  AN ,      U.  S .  A. 


1 


However,  it  does  disconnect  the  motor  if  an  overload  occurs 
which  may  be  injurious  to  the  motor  or  machine.  It  also 
functions  to  shut  down  the  motor  on  partial  failure  of  power 
lines,  that  is,  failure  of  one  line  which  would  allow  the  motor 
to  operate  on  single  phase.  On  the  larger  sizes  the  transfor- 
mers are  not  mounted  in  the  same  case  with  the  switching 
mechanism,  but  the  operation  and  functions  are  the  same  in 
all  cases. 


Bulletin  9141. 


Manual  Starters,  Slip-Ring  Motors 

Secondary  resistor  type,  Bulletin  9126,  up  to  and  including 
25HP-280  volts  and  50HP-300  volts  rotor  limitations. 

These  starters  are  of  the  sliding  contact  type,  arranged  to 
cut  out  starting  resistance  in  the  rotor  circuit.  They  are  me- 
chanically released,  and  have  no  "dead"  point.  To  stop  the 
motor,  it  is  necessary  to  return  the  lever  to  the  starting  point 
and  open  the  main  line  switch.  If  a  magnetic  main  line  switch 
is  used,  it  can  be  interlocked  with  the  starter  so  that  it  closes  on 
the  first  starting  point  and  opens  when  the  lever  is  returned  to 
the  original  position.  Care  should  be  taken  so  as  not  to  exceed 
the  rotor  limitations  given  in  the  Bulletin. 


Bulletin  9126.  With  cover  removed. 


AND    CONDENSERS    FOR    EVERY  SERVICE 


247 


Multiple  switch  motor  starter,  Bulletin  9131,  up  to  and 
including  2000  HP. 

These  starters  are  of  the  secondary  resistor  type  and 
consist  of  a  slate  panel  containing  a  number  of  levers,  which, 
when  closed  in  sequence,  cut  out  steps  of  resistance  in  the  rotor 
circuit  to  bring  the  motor  up  to  speed.  The  levers  are  so  in- 
terlocked that  they  can  only  be  closed  in  "sequence.  Up  to 
200HP,  the  resistor  is  in  the  same  enclosing  case  with  the  panel. 
The  larger  sizes  have  the  resistor  separately  mounted. 


Bulletin  913L 


A.  C.  Automatic  Starters,  2  or  3  Phase 
Squirrel  Cage  Motors 

Across-the-line  type  automatic  starters,  Bulletin  9586,  for 
capacities  up  to  150  amperes,  at  550  volts. 

These  starters  consist  of  a  positive  acting  three  or  four 
pole  magnetic  contactor,  and  C-H  thermal  overload  relays 
mounted  on  a  panel  in  a  split  case.  The  smallest  size,  for 
motors  up  to  5HP,  has  roller  type  contacts  and  is  provided 
with  a  two  button  control  switch  in  the  cover.  Larger  sizes 
have  finger  type  contacts  and  are  supplied  with  one  pushbutton 
master  switch  for  three  wire  control.  C-H  Thermal  Overload 


248 


ATTLE      CREEK.     MICHIGAN,      U.  S.  A. 


Relays  provide  ideal  protection.     When  a  relay  is  tripped,  it 
can  be  reset  by  pushing  a  button' on  the  outside  of  the  case. 


Bulletin  9586,  TypeAAA. 


Bulletin  9586, 
Types  AA  and  A. 


Primary  resistor  type  automatic  starters,  Bulletin  9605, 
up  to  and  including  30HP-220,  440  or  550  volts,  2  or  3  phase. 

These  starters  are  identical  with  those  listed  for  single 
phase  service,  except  that  for  polyphase  motors,  all  three  poles 
are  used.  They  can  be  controlled  by  any  type  of  three  wire 
or  two  wire  master  switch. 


Bulletin  9605. 


Auto  transtormer  type  automatic  starter,   Bulletin  9621, 
up  to  and  including  30HP-220  volts  and  40HP-440  or  550  volts. 

These  starters  consist  of  a  three  pole  and  a  five  pole  mag- 


249 


net ic  contactor,  and  C-H  Thermal  Overload  Relays  mounted 
on  a  slate  panel  in  a  split  enclosing  case.  On  starting,  the  five 
pole  contactor  closes,  connecting  the  motor  to  the  line,  thru  the 
auto  transformer.  After  a  definite  time  interval,  determined 
by  an  oil  dashpot,  the  three  pole  contactor  closes,  connecting 
the  motor  across-the-line.  Both  low  voltage  and  over-load 
protection  are  provided. 


Bulletin  9621. 


With  cover  removed. 


Transformer  type  automatic  starters,  Bulletin  9622,  for 
2200  volt  circuits,  up  to  and  including  400HP. 

These  starters  consist  of  a  three  pole  and  a  five  pole  oil 
immersed  magnetic  main  line  contactor,  a  solenoid  operated 
dash  pot  timing  relay,  two  control  relays  and  an  auto  trans- 
former. The  operation  is  similar  to  Bulletin  9621,  the  large 
contactor  being  operated  thru  the  control  relays.  Any  type 
of  two  wire,  or  three  wire  master  switch  can  be  used  for  control. 


Bulletin  9622. 


250 


t 

B  ATTLE 

C 

RE 

EK. 

M 

ICH 

I  C  ATM  .      U. 

S. 

A. 

r 

A.  C.  Automatic  Starters,  2  or  3  Phase  Slip- Ring  Motors 

Secondary  resistor  type  automatic  starter,  Bulletin  9633, 
up  to  25HP-110  volts,  50HP-220  volts  and  75HP-440  or  550 
volts.  These  starters  are  for  wall  mounting.  They  consist 
of  a  three  pole  magnetic  main  line  contactor  and  one  or  more 
three  pole  accelerating  contactors.  C-H  thermal  overload 
relays  provide  ideal  overload  protection  at  all  times.  Low- 
voltage  release  is  also  provided. 

On  starting,  the  accelerating  contactors  close  in  rotation, 
cutting  out  steps  of  resistance  in  the  secondary  circuit.  The 
main  line  contactor  then  closes,  connecting  the  motor  directly 
to  the  supply  lines.  In  selecting  a  starter  of  this  type,  care 
should  be  taken  so  that  the  secondary  current  rating  is  not 
exceeded.  They  can  be  controlled  by  any  type  of  two  or  three 
wire  master  switch. 


BuilecLi  9o33. 


Secondary  resistor  type  automatic  starters,  Bulletin  9638, 
up  to  and  including  1000HP-2200  volts. 

These  starters  operate  similar  to  the  Bulletin  9633  starters, 
except  that  they  are  built  for  higher  voltages — up  to  2200  volts. 
The  main  line  contactor  is  a  three  pole  oil-immersed  magnetic 
contactor  and  the  accelerating  contactors  are  two  pole.  Con- 
trol relays  govern  the  closing  of  these  contactors.  They  can 


be  controlled  by  any  type  of  two  wire  or  three   wire   master 
switch. 


Bulletin  9838. 


C.  H.   Accessories 

Pushbuttons 

These  pushbutton  stations  are  for  use  in  the  control  circuit 
of  alternating  or  direct  current  automatic  starters,  to  control 
the  various  operating  functions  of  the  controller. 

Bulletin  10250H30  is  a  single  button  switch,  intended  for 
use  as  an  auxiliary  in  connection  with  control  stations  of  the 
two  button  type. 

Bulletin  10250H26  is  a  two  button  control  station,  used 
for  starting  and  stopping  the  equipment  from  a  remote  point. 
The  "stop"  button  can  be  locked  in  the  down  position,  pro- 
viding a  "safe"  feature. 

Bulletin  10250H56  is  a  two  button  control  station  used 
for  starting  and  stopping  from  a  remote  point.  It  does  not 
provide  the  "safe"  feature. 


Bulletin  10250H30  Bulletin  10250H26  Bulletin  10250H56 


252 


1 

B  ATTLE 

C 

REE 

K. 

MICH 

IG 

AN. 

U. 

S. 

A. 

1 

Diaphragm  type  pressure  regulator,  Bulletin  10001  for 
pressures  above  atmosphere  only. 

This  pressure  regulator  is  of  the  diaphragm  type,  single 
pole,  for  handling  control  circuits  only,  having  a  maximum 
capacity  of  175  pounds  and  arranged  for  use  with  any  of  the 
self-starters. 

These  regulators  are  manufactured  in  four  different  sizes 
for  various  pressures.  In  selecting  these  regulators,  be  careful 
that  the  ranges  between  opening  and  closing  are  not  exceeded. 


Bulletin  10001. 


With  cover  removed. 


Diaphragm  type  pressure  regulators,  two  pole,  Bulletin 
10004. 

This  is  a  two  pole,  diaphragm  type,  regulator,  for  use  with 
small  A.C.  or  D.C.  motors  which  can  be  connected  directly  to 
the  line  to  start.  It  handles  the  main  line  circuit,  and  no  other 
starter  is  required.  An  unloader  device  can  be  provided  for 
air  compressor  work.  This  device  relieves  the  back  pressure 
against  the  compressor  during  starting.  Pressure  limitations 
or  HP  ratings  given  in  the  Bulletin  should  not  be  exceeded. 


Bulletin  10004. 


Witn  cover  removed. 


253 


Diaphragm  type  vacuum  regulators,   Bulletin  10005. 

These  regulators  are  similar  in  design  to  the  pressure  type, 
Bulletin  10001  but  are  arranged  for  pressures  below  atmosphere 
only,  with  a  maximum  vacuum  range  of  28  inches  of  mercury. 
These  vacuum  regulators  are  suitable  for  use  with  any  of  the 
automatic  starters,  but  as  in  the  case  of  pressure  regulators,  it 
is  necessary  to  see  that  the  maximum  and- minimum  range  be- 
tween opening  and  closing  does  not  exceed  the  limits  tabulated 
in  the  bulletin. 


Bulletin  10005. 


With  cover  removed. 


Gauge  type  pressure  regulators,  with  relay,  Bulletin  10013. 
These  gauge  type  pressure  regulators  are  for  use  with  systems 
having  a  greater  pressure  range  than  can  be  handled  by  the 
diaphragm  type,  and  are  suitable  for  use  with  any  of  the  "A.C" 
or  "D.C."  automatic  starters. 


Bulletin  10313. 


254 


B  ATTLE 

C 

RE 

CS3S3COUOC 

EK. 

MIC 

H 

IG 

AN. 

U. 

S. 

A. 

"11 

Enclosed  type  float  switches,  Bulletin  10036,  two  or  four 
pole.  These  switches  can  be  used  as  pilot  devices  in  connection 
with  A.C.  or  D.C.  automatic  starters,  or  they  can  be  used  to 
connect  small  A.C.  motors  directly  across-the-line.  Six  types 
of  mounting  can  be  supplied,  to  suit  local  conditions.  These 
float  switches  can  be  arranged  for  either  tank  or  sump  opera- 
tion. 


Bulletin  1003J. 


With  cover  removed. 


255 


I  ML  JliL  XL  JKL  Jil  JUL  JUL 


Pumps 


Direct  Acting 
Steam  Pumps 


SECTION  FIVE 


IL 

u 

N 

I  0 

N 

S 

TE 

AM 

P 

UM 

P 

COM  P  ANY 

Direct  Acting  Steam  Pumps 

The  direct-acting  steam  pump  is  one  in  which  the  water 
end  is  placed  centrally,  or  directly  in  line  with  the  steam  end. 
The  water  piston  and  the  steam  piston  are  placed  on  the  same 
rod,  and  both  operated  together  independently  of  any  crank 
movement. 

.   Direct-acting  steam  pumps  are  classified  according  to  the 
water  end  as  follows : 

Single  Double  Acting:  This  type,  which  is  illustrated  in 
figure  95,  is  the  simplex  design ,  having  one  steam  piston  operat- 
ing one  water  piston.  The  water  cylinder  is  double  acting,  in 
other  words  each  stroke  of  the  piston  causes  a  filling  at  one  end 
of  the  pump  cylinder,  and  a  discharge  at  the  other  end  of  the 
cylinder. 

Duplex  Double  Acting:  This  type  illustrated  in  figure  98, 
consists  of  two  steam  pistons  operating  two  water  pistons.  The 
steam  and  water  cylinders  are  operated  side  by  side,  and  the 
steam  valve  of  one  side  is  actviated  by  the  companion  pump. 
The  ws,ter  cylinders  are  double  acting,  in  other  words  each 
stroke  of  the  piston  causes  a  filling  at  one  end  of  the  pump 
cylinder,  and  a  discharge  at  the  other  end  of  the  cylinder. 

The  above  pumps  may  also  be  sub-divided  as  follows: 

Horizontal  Double  Acting  Pumps 

Piston  Packed  Pumps. 

Outside  Center-Packed  Plunger  Pumps. 

Outside  End-Packed  Plunger  Pumps. 

Vertical  Double  Acting  Pumps 

Piston  Packed  Pumps. 
Outside  Center-Packed  Plunger  Pumps. 
Outside  End-Packed  Plunger  Pumps. 

Direct  acting  steam  pumps  are  classified  according  to  the 
steam,  end  into  simple  and  compound. 

The  above  types  comprise  the  direct-acting  steam  pumps, 
which  are  generally  encountered.  There  are  other  types,  but 
they  are  special,  and  not  considered  of  sufficient  importance  to 

enumerate. 


258 


BATTLE       CREEK.     MICHIGAN, 


Fig.   95 

Single  Pumps 

The  characteristic  feature  of  single  pumps  is  the  valve 
motion,  or  mechanism  introduced  to  reverse  the  motion  of  ',hc 
pump. 

This  valve  motion  generally  consists  of  an  auxiliary  valve, 
figure  96,  mechanically  operated  by  the  steam  piston  and  con- 
trolling an  auxiliary  piston,  which  in  turn  operates  the  main 
valve.  The  latter  operates  the  steam  piston,  thus  completing 
the  cycle.  These  four  elements  can  always  be  recognized  in  a 
single  pump. 

There  are  numerous  types  of  valve  motions  employed  on 
single  pumps,  but  the  most  satisfactory  is  that  type  in  which 
the  steam  piston  is  controlled  by  a  slide  valve,  the  valve  itself 
being  operated  by  an  auxiliary  steam  piston  working  in  its  own 
chest,  and  the  auxiliary  piston  being  moved  by  the  direct  ap- 
plication of  steam  pressure. 

The  admission  of  the  sceam  to  the  end  of  the  auxiliary 
steam  piston  in  the  chest  is  controlled  by  a  flat-faced  auxiliary 
slide  valve  in  the  chest,  which  is  actuated  by  an  external  valve 
mechanism  from  the  piston  rod.  As  the  pump  reaches  the  end 
of  the  stroke,  steam  is  admitted  by  the  auxiliary  valve  to  one  end 
of  the  auxiliary  piston,  while  the  other  end  is  put  into  communi- 
cation with  the  exhaust  at  the  same  time,  and  the  difference  of 
pressure  in  the  two  ends  causes  the  auxiliary  piston  to  move 
instantaneously  the  full  distance  of  its  travel,  carrying  the  main 


259 


|"       UN 

I  O  N 

STEAM 

PUMP 

COM  P  ANY 

4 

slide  valve  with  it,  and  thus  reversing  the  stroke  of  the  pump. 
As  the  main  valve  is  operated  by  the  force  of  live  steam,  there 
is  no  hesitancy  of  action  and  no  dead  point,  the  piston  is  reversed 
instantaneously,  and  always  at  the  same  point  of  its  stroke 
regardless  of  the  load. 

The  Burnham  valve  gear,  which  is  the  type  referred  to  is 
described  in  detail  on  the  following  pages. 

Burnham  Steam  Pump 

Sectiona.  Views  of  Steam  Cylinder,  Steam  Chest  and  Valves. 


VALVE  STEM  STUF- 
FING BOX.  SCREWED 
TYPE,  OF  LIBERAL 
DEPTH 


AUXILIARY  STEAM  VALVE  — FLAT  FACE  SLIDE 

STEAM  CHEST  VALVE  —  ALWAYS  TIGHT  —  CANNOT  WEAR  TO 

MAIN  PORT  A  SHOULDER  —  THIS  VALVE  IS  OPERATED  BY 

THE  ACTUATING  LEVER  FROM  THE  PISTON  ROD 


MAIN  STEAM  VALVE  — FLAT  FACE 

SUDE  VALVE  —  ALWAYSTIGHT          CTC/IM  IHI  KT 

CANNOT  WEAR  TO  A  SHOULDER 

STEAM     DRIVEN    BY 

AUXILIARY  PISTON 

STEAM  THROWN  AUX- 
ILIARY PISTON  FOR 
OPERATING  MAIN 
SLIDE  VALVE 

PREADMISSION 
STEAM  PORT 
FOR  STARTING 
PISTON. 

MAIN  STEAM 
PORT 


AUXILIARYPISTON  FITTED 
WITH  SELF-ADJUSTING 
SNAP  RINGS 


STEAM  PISTON  FITTED 
WITH  TWO  SELF-AD- 
JUSTING  SNAP  RINGS 


STEAM  CYLINDER  FOOT  OF 
LIBERAL  SIZE  —  PLANED 
ON  BOTTOM 


VALVE    GEAR    CONSTRUCTION     IS    SUCH 
THAT  PISTON   MUST  COMPLETE  ITS  FULL 
STROKE    BtFORL    IT  CAN    REVERaE 
CAM  BLOCKS  FOR  ADJUST- 
ING    STROKE  — CAN     BE 
CHANGED    WHILE    PUMP, 
IS    IN    OPERATION 


CAM  BLOCK  AD- 
JUSTING NUTS 

ACTUATING  LEVER 
OPERATING  AUX- 
ILIARY STEAM 
VALVE 


LIBERAL 
SIZE  PISTON 
ROD 


STEEL  ROLLER 


CROSSHEAD 


DEEP  STUFFING    BOX  WITH  BOLTED 
GLAND  ON  6- INCH  DIAMETER  CYLIN- 
DER   AND    LARGER.    AND    SCREWED 
GLAND    CN    SMALLER  SIZES 
CYLINDER  DRAIN  COCK 


STEAM  CYLINDER  WALLS  ARE  HEAVY 
ENOUGH    TO    STAND     RE-BORING 

TWICE 


Fig.  96 


260 


Burnham  Direct-Acting  Steam  Pumps 

Operation 

The  following  is  a  short  description  of  the  Burnham  Steam 
Valve  and  its  operation,  as  illustrated  by  the  cuts  on  the  preced- 
ing page. 

The  top  view  of  the  steam  cylinder  shows  the  auxiliary 
valve  and  chest  in  section. 

The  lower  view  shows  a  vertical  section  through  the  steam 
cylinder. 

Live  steam  enters  the  steam  chest  at  the  top  and  is  ad- 
mitted to  the  cylinder  alternately  through  the  main  steam  ports. 

At  the  beginning  of  the  stroke  the  main  steam  port  is  covered 
by  the  piston  as  shown  in  the  cut.  A  preadmission  port  is  pro- 
vided which  admits  only  enough  steam  to  give  the  steam  piston 
an  easy  start,  but  when  the  steam  piston  has  moved  far  enough 
to  uncover  the  main  port,  it  receives  the  full  steam  pressure  and 
moves  at  its  normal  speed  until  it  covers  the  main  port  at  the 
other  end  of  the  cylinder,  when  it  traps  the  remaining  exhaust 
steam  in  the  cylinder  and  thus  forms  a  cushion,  giving  the  steam 
piston  an  easy  stop. 

The  valve  gear  is  positive  in  action,  and  is  operated  by  the 
actuating  lever  moved  by  a  roller  attached  to  the  piston  rod. 
Ihis  lever  alternately  moves  the  cam  blocks  both  of  which  are 
fastened  to  the  auxiliary  valve  stem,  which  in  turn  moves  the 
auxiliary  valve  in  the  direction  opposite  to  the  motion  of  the 
piston. 

When  the  steam  piston  completes  its  stroke,  the  actuating 
lever  moves  the  auxiliary  valve,  opening  first  the  chest  pre- 
admission port,  then  the  chest  main  port,  admitting  live  steam 
to  one  end  of  the  auxiliary  piston  and  at  the  same  time  opening 
the  auxiliary  exhaust  at  the  opposite  end,  thus  causing  the 
auxiliary  piston,  which  carries  the  main  valve,  to  move,  revers- 
ing the  motion  of  the  pump. 

The  cam  blocks  are  independently  adjustable  on  the 
auxiliary  valve  stem  enabling  the  engineer  to  make  the  piston 
run  as  close  to  the  heads  as  he  desires,  and  to  make  adjust- 
ment to  compensate  for  wear. 

The  advantages  of  this  valve  gear  are:  a  momentary 
pause  of  the  piston  at  the  end  of  each  stroke,  causing  the 
water  valves  to  seat  quietly  without  shock  or  jar;  a  slow  initial 
movement  of  the  piston,  whereby  the  water  columns  are  started 
gradually,  relieving  the  pump  and  piping  of  undue  strains;  a 


261 


UNION       STEAM 

63^^ 


P  U  M  P       CO  M  P  ANY 


steam  pressure  on -the  main  steam  piston  proportioned  to  the 
amount  of  work  that  it  has  to  do;  and  immunity  from  damage 
in  case  of  accident. 


36 


Fig.  97 

Sectional  View  of  Burnham  Pump. 

Directions  for  Setting  the  Burnham  Valve 

All  Burnham  pumps  are  carefully  tested  at  the  factory 
under  working  conditions  and  the  valve  gear  is  properly  set.  If 
it  becomes  necessary  to  readjust  the  valve  gear,  proceed  as 
follows : 

On  yoke  68  ( see  figure  97),  upon  which  moves  the  piston-rod 
guide  92,  will  be  found  a  mark  at  each  end,  indicating  the  extreme 
travel  of  the  piston. 

If  the  pump  does  not  run  as  close  to  the  mark  as  practical, 
loosen  the  nuts  on  the  valve  stem  and  the  set  screw  in  cam  block 
109  on  the  opposite  side  (of  the  actuating  lever  106)  from  which 
it  is  desired  to  lengthen  the  stroke,  and  move  the  cam  block 
away  from  the  point  of  contact  of  actuating  lever  106. 

This  will  allow  the  piston  to  move  farther  before  opening 
the  valve. 

It  will  be  found  that  by  moving  this  cam  block  iV  of  an 
inch,  it  makes  quite  a  perceptible  difference  in  the  piston  travel, 
according  to  the  size  of  pump  to  be  adjusted. 

If  the  pump  should  travel  too  close  to  the  marks,  which 
would  cause  it  to  hesitate  and  stop  at  the  end  of  stroke,  then 
move  these  cam  blocks  109  toward  the  point  of  contact  of  actuat- 
ing lever  106. 


--fe^ 


2.62 


Always  move  the  cam  blocks  on  the  opposite  side  of  lever 
from  which  it  is  desired  to  change  the  stroke. 

In  all  cases  the  piston  should  make  as  long  a  stroke  as 
possible  and  give  the  required  speed  to  do  the  work. 

To  locate  the  marks  on  the  yoke,  indicating  the  extreme 
travel  of  the  piston,  move  the  steam  piston  to  one  end  till  it 
strikes  the  cylinder  head  and  mark  with  a  prick  punch  the  yoke 
on  which  the  piston  rode  guide  92  rides.  Repeat  this  operation 
on  the  other  end,  and  use  these  marks  to  adjust  the  valve  as 
described. 

Advantages  of  Single  Pumps 

The  single  pump  is  the  most  desirable  type  of  direct  acting 
pump  because  of  its  simplicity,  reliability  and  economy  in 
operation  and  maintenance. 

The  single  pump  is  simple  in  construction  and  has  a  com- 
paratively few  number  of  moving  parts  and  packed  joints, 
with  the  result  that  there  is  a  large  saving  in  friction.  The  few 
number  of  moving  parts  required  in  the  single  pumps  means 
less  wear  and  less  liability  to  accidents  and  slippage  and  shut- 
downs for  repairs,  as  well  as  entailing  less  care  on  the  part  of  the 
operating  engineer  to  see  that  the  parts  are  in  the  proper  running 
condition. 

It  is  a  well-known  fact  that  the  chief  sources  of  loss  in  any 
steam-actuated  machine  are  those  by  direct  radiation  through 
the  walls  of  the  cylinders,  and  by  condensation  of  the  steam 
on  the  walls  during  admission,  with  subsequent  re-evaporation 
during  exhaust.  Such  heat  losses  mean  of  course  wasted  energy. 
As  the  radiating  surface  increases,  the  loss  of  energy  increases 
with  it,  and  as  a  single  pump  has  a  minimum  radiating  surface, 
the  heat  losses  are  a  minimum. 

In  the  direct-acting  steam  pump,  all  steam  used  to  fill  the 
port  passages  of  the  cylinder,  and  the  clearances  at  the  end  of  the 
stroke,  is  wasted  as  it  is  rejected  to  the  exhaust  without  having 
done  any  work.  Clearance  is  a  necessary  evil,  so  it  is  made  as 
small  as  possible  with  due  regard  to  proper  running  of  the  pump. 
Single  pumps  are  made  with  but  one  steam  port  at  each  end  of 
the  cylinder,  and  this  reduces  the  wasted  steam  space  to  a 
minimum. 

The  greatest  advantage  of  the  single  pump  as  regards 
steam  consumption  lies  in  the  fact  that  with  its  valve  motion, 
it  has  to  complete  its  full  stroke  before  it  can  reverse.  This 
means  that  the  waste  steam  space  at  the  end  of  the  stroke 
which  is  the  source  of  greatest  loss  in  a  pump  is  minimized. 


AND    CONDENSERS    FOR    EVERY  SERVICE 


fp      UNION 

STEAM 

P  UM  P 

COM  P  ANY 

J 

Fig.  98. 
Duplex  Piston  Pump. 

Duplex  Pumps 

Duplex  pumps  are  characterized  by  the  arrangement  of 
cylinders  and  type  of  valve  gear.  The  universal  arrangement 
is  to  place  two  pumps  side  by  side,  the  main  steam  valve  of  one 
side  being  actuated  through  a  system  of  levers,  rods  and  links 
from  the  piston  rod  of  the  other  side.  In  designating  the  side 
of  a  duplex  pump,  it  is  customary  to  call  the  right  side  when 
•standing  at  the  steam  end  f acting  the  water  end  of  the  pump, 
the  "Right  Hand  Side,"  and  that  to  the  left,  the  "Left  Hand  Side." 

Valve  Motion 

The  sectional  view,  figure  99,  which  illustrates  the  Union 
duplex  pump,  shows  the  type  of  valve  gear  generally  employed 
on  duplex  pumps.  The  steam  valves  Q  and  I  are  ordinary  D 
slide  valves.  The  valve  motion  is  transmitted  from  the  pistons 
to  the  valves  by  two  rock-shafts  C  and  D  mounted  on  the  valve 
gear  bracket  G.  To  the  right  hand  end  of  the  upper  rock-shaft 
C  is  fitted  a  long  arm  A,  the  lower  end  of  which  is  attached  to  the 
crosshead  H  on  the  piston  rod.  To  the  left  hand  end  of  the  rock 
shaft  C  is  fitted  the  long  crank  B  attached  to  the  valve  rod  S 
by  means  of  a  coupling  and  link  P. 

To  the  left  hand  end  of  the  lower  rock-shaft  D  is  fitted  a 
short  arm  E.  To  the  right  hand  end  of  the  lower  rock  shaft 
D  is  fitted  the  short  crank  F  attached  to  the  valve  rod  J  by 
coupling  and  link  K. 


J.-...-.»rH.«n»>jirTirTr^;.Trr.3..-.».-.Tr«n«J»n«>or^gTI-  i  c»  «  n  B  a  B  XTfATB 

PUMPING    MACHINERY,    AIR   COMPRESSORS         I 


264 


Thus  the  valve  I  on  the  right  hand  pump  is  operated  through 
the  valve  rod  J,  link  K,  crank  F,  rock-shaft  D,  arm  E,  piston 
rod  O,  and  piston  N.  The  valve  on  the  left  hand  pump  is  operated 
through  the  valve  rod  S,  link  P,  crank  B,  rock-shaft  C,  arm  A , 
piston  rod  M,  and  piston  L. 

On  the  duplex  purnp,  the  valve  motion  is  such  that  one  side 
finishes  its  stroke,  and  waits  for  its  valve  to  be  moved  by  the 
other  side  of  the  pump,  before  it  can  start  on  its  return  stroke. 
This  pause  allows  the  water  valves  to  seat  quietly  and  obviates 
shocks.  As  one  or  the  other  of  the  steam  valves  is  always  open, 
there  is  no  dead  center,  and  the  pump  will  start  whenever  the 
steam  is  turned  on. 


UNION       S  TEAM      ~TMJM  I'^^C^O  M^P  ANV  ' 

nUnrBra  vvWW*' gWw  w »v  a*  t  u  * tu  <rvTfvTrin~irfTrrv* ~ei>*v  ivy  VTrb  \ 


Directions  for  Setting  Steam  Slide  Valves 
of  Duplex  Pumps 

To  set  the  Slide  Valves  of  Duplex  Pumps  without  outside  ad- 
justment.— First  open  drip  cocks  so  that  steam  cylinders  will  be 
drained ;  then  move  piston  rod  of  one  side  toward  steam  cylinder 
head  by  prying  against  crosshead  until  steam  piston  strikes  head 
and  then  make  a  mark  on  piston  rod  close  to  face  of  steam  piston 
rod  gland.  Next  move  piston  rod  to  opposite  end  of  stroke  until 
steam  piston  strikes  and  make  a  mark  on  piston  rod  just  half  way 
between  first  mark  and  face  of  steam  piston  rod  gland.  Now 
move  piston  rod  backward  until  second  mark  is  flush  with  face 
of  steam  piston  rod  gland  and  the  piston  will  stand  at  half  stroke. 
Disconnect  link  from  knuckle  of  valve  rod  on  opposite  side  and 
place  slide  valve  in  steam  chest,  chest  cover,  of  course,  having 
been  taken  off  for  this  purpose,  so  that  valve  exactly  covers  both 
steam  ports  that  lead  to  opposite  ends  of  cylinder 

Now  hold  slide  valve  nut  exactly  in  centre  of  space  between 
slide  valve  lugs,  screw  valve  rod  through  this  nut  until  knuckle 
eye  is  in  line  with  link  eye,  and  push  link  pin  in  place.  Repeat 
this  process  with  other  side  of  pump  and  the  operation  is  com- 
plete. It  will  be  found  an  advisable  plan  to  move  both  pistons 
to  middle  stroke  before  touching  either  slide  valve. 

Before  putting  on  the  steam  chest  covers,  move  one  of  the  slide 
valves  so  as  to  open  the  steam  port,  otherwise  the  pump  might  not 
start^as  in  setting  the  valves  the  steam  ports  have  been  covered. 

All  steam  valves  are  properly  set  before  the  pumps  leave 
the  factory. 

Advantage  of  Duplex  Pumps 

The  advantage  of  a  duplex  pump  over  other  types  of  direct 
acting  pumps  is  its  continuous  discharge.  The  stroke  of  one 
piston  begins  before  the  other  piston  has  come  completely  to 
rest,  so  the  movement  of  the  suction  and  discharge  columns  is 
practically  continuous. 


PUMPING    MACHINERY^AIR    CQ_MP_RESS  Q_RS- 

cs^ir^rir'ff  *s  A^'iuS^'u.  "Ofx~M  jj'>"tf  ^"gr^ygTr^gy  y^nygggw  wy  ya^n^tf  pwgj^x'ygTriirrig'c'-tt  •a-it^M-g'^x^^s^g'g'g  yir 


266 


B  ATTLE 

C 

RE 

EK. 

MIC 

HI 

G 

TTJTi 

AN, 

U. 

S. 

A. 

3 

Horizontal  Piston  Pumps,  Simplex  Design 

Horizontal  piston  packed  pumps  are  generally  built  for 
fluid  pressures  of  100  to  150  pounds  per  square  inch,  although 

the  smaller  sizes  are  suitable  for  working  pressures  up  to   250 
pounds  per  square  inch. 

Pumps  of  the  piston  packed  pattern  are  built  with  the  suc- 
tion and  discharge  valve  decks  arranged  above  the  piston. 
Small  pumps  of  this  type  have  the  suction  and  discharge  open- 
ings on  either  side  as  shown  in  figs.  95a  and  95b,  or  the  suction 
on  one  side,  and  discharge  on  the  other,  as  shown  in  fig.  100. 


Fig    100 

.onzontal  Piston  Pump  with 
suction  cne  side,  discharge 
the  other 


*•*-:•••  •--.'-•• 
Pig.  95b. 

Section  of  fluid  end  showing  suction  and 
discharge  openings  either  side. 


AND 

CONDENSERS 

FOR 

F 

VERV 

S 

ERVICE 

4 

267 


IT-UN 

I  O  N 

STEAM 

PUMP 

COM  P  ANY 

3 

These  pumps  are  fitted  with  either  a  pressed  bronze  liner, 
or  a  bolted  removable  bronze  flanged  liner. 

On  these  small  sizes  of  piston  pumps  there  is  not  sufficient 
room  for  hand  plates,  so  access  to  the  valves  is  gained  by  remov- 
ing the  hood  and  valve  plate. 


Fig.  lOla, 

Horizontal  Piston  Pump,  Hand-Plate 
Design. 


Fig.  lOlb. 

Section  of  Fluid  End, 
Hand-Plate  Design. 


The  larger  sizes  of  piston  pumps  have  the  fluid  end  of  the 
hand-plate  design,  as  shown  in  figs.  lOla  and  lOlb.  Here  the 
valves  are  all  accessible  by  the  removal  of  the  hand  plates. 
These  large  cylinders  are  always  provided  with  the  flanged  type 
of  removable  liners. 


102a 

Horizontal  Duplex  Piston  Pump, 
Suction  Opening  on  Side,  Discharge 
at  End. 


1NE  R.Y, 


268 


i 


CREEK.     MICHIGAN.      U.S. 


Fig.  102b. 

Section  of  Fluid  End  of  Duplex 
Piston  Pump,  Showing  Suction 
Either  Side,  Discharge  at  End. 


Horizontal  Piston  Pumps,  Duplex  Design 

Duplex  Piston  Pumps  are  built  for  fluid  pressures  up  to 
250  pounds  per  square  inch,  the  pressure  depending  on  the  size 
of  pump. 

On  small  duplex  pumps,  the  fluid  end  is  of  the  type  as  shown 
in  figures  102a  and  102b,  103a,  103b.  The  suction  opening  is 
arranged  either  on  the  sides  or  at  the  end  of  the  cylinder,  and 
the  discharge  is  at  the  end  of  the  cylinder.  These  cylinders 
are  fitted  with  bronze  liners  either  bolted  or  pressed  depending 
on  the  size.  The  valves  are  accessible  by  the  removal  of  the 
hood  and  valve  plate. 

Large  sizes  of  duplex  pumps  have  the  fluid  end  of  the  hand- 
plate  design  as  shown  in  figure  104.  All  valves  are  accessible 
by  removal  of  the  hand  plates.  These  pumps  are  fitted  with 
bronze  bolted  liners. 


Fig.  103a 
Horizontal  Duplex  Piston  Pump,  Suction  and  Discharge  at  end 


AND    CONDENSERS    FOR    EVERY  SERVICE 

rirv-ira^nrfi 


269 


Fig.  103b. 

Section  of  Fluid  End  of  Duplex  Piston  Pump,  showing  end 
Suction  and  Discharge. 


Fig.  202. 
Section  of  Duplex  Piston  Pump,  Hand-Plate  Design. 


PUMPING 


270 


K 

B  ATTLE 

C 

RE 

EK, 

M 

ICH 

IG 

AN, 

U. 

S. 

za 

Outside  Center-Packed  Pumps 

For  fluid  pressures  higher  than  150  pounds,  and  up  to  300 
pounds  pressure,  the  outside  center-packed  plunger  pump,  as 
illustrated  in  fig.  105a  is  generally  used. 

In  this  type  of  pump  the  plunger  glands  are  easily  accessible, 
and  any  leakage  from  the  plunger  can  be  detected,  and  stopped 
while  the  pump  is  in  operation. 

In  the  center  packed  plunger  pump,  the  suction  valves  are 
located  below  the  plunger,  and  the  discharge  valves  are  above. 
All  valves  are  accessible  by  the  removal  of  the  hand  plates. 

In  the  small  sizes,  the  fluid  cylinder  is  of  the  type  as  shown 
in  fig,  105b,  wrhile  in  the  larger  sizes  the  cylinders  are  bolted 
together  as  shown  in  fig  106 


Fig,  105a 
Outside  Center-Packed  Pump. 


Fig.  105b 

Section  of  Fluid  End  of  Outside  Center-Packed  Pump,  used  on 
smaller  sizes. 


AND    CONDENSERS    FOR    EVERY   SERVICE 


271 


UNION       STEAM       PUMP       COMPANY 


I 


Fig.  106. 

Section  of  Fluid  End  of 

Outside  Center-Packed  Pump, 

used  on  large  sizes. 


Outside  End- Packed  Plunger  Pumps 

For  fluid  pressures  up  to  150  and  250  pounds  per  square 
inch,  the  end-packed  plunger  type  of  pump  as  shown  in  fig.  107a 
is  very  often  used. 

In  this  type  there  are  two  plungers  connected  by  side  rods. 
The  plunger  glands  are  readily  accessible,  and  any  leakage 
from  the  plungers  can  be  detected  and  stopped,  while  the  pump 
is  operating. 

The  outside  end-packed  fluid  cylinder  is  of  the  valve- 
plate  design.  In  the  smaller  sizes  the  valves  are  accessible  by 
the  removal  of  the  hood,  and  the  valve  plate  fig.  107b.  The 
larger  sizes  have  hand  plates  for  gaining  access  to  the  valves  as 
shown  in  fig.  108. 


Fig   107a 
Outside  End-Packed  Plunder  Pump 


272 


Fig.  107b 

Section  of  Fluid  End  of  Outside  End-Packed  Plunger  Pump, 
small  sizes. 


Fig.  108. 
Outside  End-Packed  Plunger  Pump,  Hand-Plate  Design. 

Pot  Valve  Pumps 

For  fluid  pressures  of  150  pounds  and  over,  the  End-Packed 
Pot-valve  Pump  as  shown  in  figs.  109a  and  203  is  used. 

On  account  of  the  high  pressures  this  type  of  pump  is  subject 
to,  the  castings  are  reduced  to  the  smallest  possible  dimensions. 
The  valve  chambers  are  small,  and  the  valves  used  are  generally 
of  the  bevel-seat  wing  type.  The  valves  are  readily  accessible 
by  removing  the  cover  over  the  valve.  See  fig.  109  b. 


273 


UNION       STEAM       PUMP 


Fig.  109a. 
Pot- Valve  Plunger  Pump 


Fig.  203. 
Duplex  Pot- Valve  Plunger  Pump. 


Fig.  109b. 

Section  of  Fluid  End  of 
Pot- Valve  Pump. 


Hydraulic  Pressure  Pumps 

For  higher  pressures  up  to  2000  pounds  per  square  inch, 
the  hydraulic  pump  with  cast  iron  fluid  end  as  shown  in  figs. 
HOa  and  HOb  is  generally  used. 

For  pressures  up  to  3000  pounds  per  square  inch,  these 
pumps  are  fitted  with  cast  steel  fluid  ends,  and  for  pressures 
above  3000  pounds,  the  fluid  ends  are  made  of  forged  steel, 
as  shown  in  Figs.  Ilia  and  lllb. 

In  the  forged  steel  cylinders  all  plunger  and  valve  openings 
are  drilled  from  the  solid  forging. 

In  hydraulic  pressure  pumps  the  valves  used  are  of  the 
bevel-seat  wing  type.  These  valves  are  accessible  by  the  re- 
moval of  the  screwed  plugs  over  the  valves. 


1C  Ij  I  G  A1N       U.  S.  A 


B  ATTLE      C  R.EEK. 


Fig.  llOa 
Hydraulic  Pressure  Pump  with  Cast  Iron  or  Cast  Steel  Fluid  End. 


Fig    HOb. 

Section  of  Hydraulic  Pressure  Pump  with  Cast  Iron  or  Cast  Steel 

Fluid  End 


Fig.  Ilia. 
Hydraulic  Pressure  Pump  with  Forged  Steel  Fluid  End. 


Fig.  lllb. 
Section  of  Hydraulic  Pressure  Pump  with  Forged  Steel  Fluid  End. 


AND    CONDENSERS    FOR   EVERY  SERVICE 


275 


y 

N 

1  0 

N 

STE 

AM 

P 

UM 

P 

COM  P  ANY 

J| 

Vertical  Piston  Pumps 

The  type  of  fluid  end  generally  used  on  piston  pumps  is  of 
the  piston  pattern  as  shown  in  the  accompanying  figures.  These 
pumps  are  suitable  for  pressures  up  to  300  pounds  per  square 
inch. 

The  design  of  the  fluid  end  is  such  that  all  valves  are  easily 
accessible  by  the  removal  of  the  side  plate.      These  pumps  are 
furnished  with  either  bronze  disc  valves  or  rubber  valves,  de- 
pending on  the  service.     Liners  are  of  bronze,  pressed  in  place 


Fig.  112a 

Single  Vertical  Pistor 
Pump. 


Fig.  112b. 

Section  of  Fluid  End  of  Single  Vertical 
Piston  Pump. 


The  vertical  pump  which  is  built  in  both  the  simplex  and 
duplex  design  is  particularly  desirable  on  account  of  the  small 
floor  space  required  and  the  fact  that  the  vertical  position  of  the 
reciprocating  parts  reduces  the  friction  and  wear  to  a  minimum. 

Vertical  pumps  are  built  with  a  base  for  floor  or  deck 
moun'cing,  or  with  brackets  for  bolting  to  the  wall  or  bulkhead. 


PUMPING    MAC HINER.V,    AIR   COMPRESSORS 


Fig.-llSa 

Vertical  Duplex  Piston  Pump. 


Fig.  113b 
Section  of  Fluid  End  of  Vertical  Duplex  Piston  Pump. 


AND    CONDENSERS    FOR    EVERY   SERVICE 


277 


1 


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P  U 

M  P 

COM  PANY 

1 

Fig.  114 

Vertical  Duplex 

Piston  Pump, 

Bulkhead 

Mounting 


Simple  Cylinder  Pumps 

Direct-acting  steam  pumps  having  only  one  (high  pressure) 
steam  cylinder  to  each  fluid  cylinder,  are  classified  as  simple 
cylinder  pumps. 

In  simple  cylinder  pumps,  the  steam  acts  with  full  pressure 
the  entire  length  of  the  stroke,  i.e.,  there  is  neither  cut  off  nor 
compression.  The  indicator  diagram  taken  from  a  simple 
cylinder  direct-acting  pump  is  practically  rectangular  as  shown 
in  figure  115. 

The  mean  effective  pressure  in  the  steam  cylinder  of  a 
simple  cylinder  pump  is  equivalent  to  the  initial  steam  pressure 
per  square  inch  minus  the  back  pressure  per  square  inch. 


Fig.  115 
Indicator  Card  of  Simple  Cylinder  Direct-Acting  Pump. 

Calculation    of   Simple   Steam    Cylinders 

In  calculating  the  size  of  simple  steam  cylinders,  it  is  neces 
sary  to  know  the  type  of  pump,  whether  piston  or  outside  packed 
plunger,  the  diameter  of  the  fluid  cylinder,  the  fluid  pressure, 
the  initial  steam  pressure,  and  the  exhaust  or  back  pressure. 


278 


Example 

Assume  we  have  a  piston  type  fluid  cylinder  12"  in  diameter, 
16"  stroke.  The  fluid  pressure  is  100  pounds  per  square  inch, 
the  initial  steam  pressure  is  110  pounds  per  square  inch,  and  the 
exhaust  or  back  pressure  is  5  pounds  per  square  inch.  It  is 
desired  to  find  the  proper  size  simple  steam  cylinder,  which  will 
be  satisfactory  for  the  conditions. 

Solution 

The  area  of  a  12  "  piston  =113  square  inches. 

113x100  =  11300  pounds  total  pressure  on  fluid  piston. 

Referring  to  page  295,  the  mechanic*!  efficiency  of  a  16 
ii  ch  stroke  piston  pump  is  80x80  =  64  per  cent.  Then  the  total 
Joad  or  pressure  to  be  exerted  by  the  steam  piston  will  be 

=  17656  pounds. 


The  initial  gauge  pressure  at  the  steam  cylinder  is  110 
I  ovnds,  and  the  back  pressure  5  pounds,  making  the  net  steam 
pressure  105  pounds. 

'Then  -  -  —  =  168.1  Square  inches. 
105 

=  Area  of  steam  piston. 

The  nearest  commercial  size  of  steam  cylinder  will  be  16 
inches,  and  the  size  of  the  pump  will  then  be  16X12x16. 

Compound  Steam  Cylinder  Pumps 

Direct-acting  steam  pumps  take  steam  during  the  entire 
stroke,  which  makes  them  extravagant  in  the  use  of  steam 
compared  with  the  amount  of  work  done. 

To  overcome  this  inherent  difficulty,  compound  steam 
cylinders  are  resorted  to  where  econgmy  is  essential.  In  com- 
pounding, however,  unless  the  boiler  pressure  is  80  pounds  or 
over,  additional  initial  expense  involved  will  not  be  warranted 
unless  the  pump  operates  condensing. 

In  compound  pumps  the  steam  is  admitted  to  the  high  pres- 
sure cylinder  during  the  entire  length  of  the  stroke,  so  that  it 
is  not  vised  expansively.  When  the  exhaust  port.  of  the  high 
pressure  cylinder  is  opened,  the  pressure  immediately  drops  to 


279 


U  N  I  ON       S  TE  AM       P  U  M  JP       CO  MPAN  Y 

^•tfVTJTrTflT^'^QfWTarf  y  vvyv^Tinrv^^Y^  f 


equalize  the  pressure  on  the  exhaust  side  of  the  high-pressure 
cylinder,  the  receiver  pipe,  and  the  low-pressure  steam  chest. 
When  the  pistons  move  on  their  return  stroke,  the  exhaust  pres- 
sure in  the  high-pressure  cylinder  falls  to  the  pressure  in  the 
low-pressure  cylinder,  this  drop  being  in  accordance  with  Boyle's 
Law,  for  the  area  of  the  low-pressure  cylinder  being  greater 
than  the  high  pressure,  as  the  pistons  advance,  the  total  volume 
increases,  and  the  steam  expanding  reduces  in  pressure.  Figure 
116  illustrates  the  indicator  card  of  a  compound  direct-acting 
pump. 


M7? 


Fig.  116 
Indicator  Card  of  Compound  Direct-Acting  Pump. 

Gain  in  Compounding 

The  percentage  of  gain  by  compounding  varies  from  25  to 
35  per  cent  in  non -condensing  pumps,  and  25  to  40  per  cent  in 
condensing  pumps,  depending  upon  the  conditions  of  operation. 

Ratio  of  Cylinders  in  a  Compound  Pump 

The  ratio  of  cylinders  in  a  compound  pump  varies  from 
two  to  three.  This  ratio  is  generally  dependent  on  the  initial 
cost,  which  is  based  on  using  standard  commercial  sizes. 

Formulae  for  Calculating  Compound  Pumps 

The  sizes  of  compound  cylinders  to  use  on  a  direct-acting 
pump  may  be  calculated  by  the  following  formula. 

In  which  I  =  Initial  absolute  steam  pressure. 
B  =  Absolute  back  pressure. 

Absolute  back  pressure  is  16  pounds  for  non -condensing 
pumps,  and  6  pounds  for  condensing  pumps. 

R=  Ratio  of  steam  cylinders. 

A  =  High  pressure  cylinder  area. 


280 


Effective  pressure,  high-pressure  cylinder=I — •  (a) 

R 

Effective  pressure,  low-pressure  cylinder  = — — B 

R 

Then  R( B  )  -I— RB  equals  (b) 


the  effective  pressure  in  the  low-pressure  cylinder  referred  to 
the  high-pressure  cylinder. 

The  sum  of  (a)  and  (b)  gives  the  total  effective  pressure 
referred  to  the  area  of  the  high-pressure  cylinder  or 

total  effective  pressure  =1—  —  + 1— RB  =21— RB 

R  R 

Hence  the  total     pressure  exerted  by  the  steam  cylinders 
of  a  compound  pump  referred  to  the  area  of  the  high-pressure 
cylinder  equals 

Ax(21— RB— —  J  (47) 


Example 

Assume  we  have  an  outside  center-packed  type  fluid 
cylinder  14  inches  in  diameter,  20  inch  stroke.  The  fluid 
pressure  is  150  pounds,  the  initial  steam  pressure  125  pounds 
gauge,  and  the  exhaust  or  back  pressure  16  pounds  absolute. 
It  is  desired  to  find  the  proper  size  compound  steam  cylinders, 
which  will  be  satisfactory  for  the  conditions. 

Solution 

Area  of  14  inch  plunger  =  154  square  inches. 

154X150  =  23100  pounds  =  total  pressure  on  fluid  plunger. 

Referring  to  page  295,  the  mechanical  efficiency  of  a  20 " 
stroke  outside  packed  pump  is  80X80=64  per  cent,  then  the 
total  load  or  pressure  to  be  exerted  by  the  steam  pistons  will  be 

23100 

. =36093  pounds. 

The  initial  steam  pressure  is  125  pounds  gauge,  or  125  + 14 . 7 
absolute. 


|     "AND 

CONDENSERS 

FOR 

EVERY 

S 

ERVICE 

-I 

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P       C  OM 

PA 

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1 

The  back  pressure  is  16  pounds  absolute.  Now,  referring 
to  formula  47,  and  substituting  the  initial  steam  pressure, 
the  back  pressure,  the  total  effective  pressure,  and  a  cylinder 
ratio  of  3 

36093=area  high-pressure  cylinder   x(  2  X  139.7  —  3  X  16 
139. 7\  \ 


36093 
Simplifying  -    —  =  195  sq.  in,  =  area   of  high  -  pressure 

cylinder. 

This  is  the  approximate  area  of  a  15^ *  cylinder. 

The  area  of  the  low  pressure  cylinder  will  then  be  195X3  = 
585  square  inches,  or  approximately  27"  diameter. 

The  nearest  commercial  sizes  will  be  16  inches  high -pressure, 
and  26  inches  low-pressure,  so  the  size  of  the  compound  pump 
in  question  will  be  16  and  26X14X20. 

The  following  table  gives  the  proper  sizes  of  steam  cylinders 
for  compound  pumps  using  steam  pressures  from  80  to  200 
pounds.  In  this  table  is  given  the  total  pressure  exerted  by 
steam  cylinders  as  calculated  by  formula  47. 

The  cylinder  ratios  given  are  standard  commercial  sizes, 
and  those  recommended  for  the  pressures  given. 

Compound  Steam  Cylinders 

Total  Pressures  exerted  by  various  sizes  with  steam  pressures  of  80-200 
pounds  'per  square  inch  gauge  pressure,  and  16  pounds  absolute  back 
pressure. 


8 

£$ 

Wi  <L> 
&|T3 

STEAM  PRESSURE 

J3  C 

s'5 

O^> 

h-30 

R 

80 

90 

130 

110 

120 

130 

140 

150 

160 

1,0 

180 

190 

200 

8 

12 

2.25 

5596 

6378 

7160 

7941 

8723 

9505 

1028  i 

11069 

11850 

126J3 

13415 

14197 

149/9 

10 

16 

2.56 

8753 

10017 

11281 

12545 

13809 

15073 

16337 

1/601 

18865 

20129 

21392 

22656 

23920 

12 

18 

.25 

12390 

14349 

16108 

17867 

19627 

21386 

23146 

24905 

26664 

28424 

30183 

31943 

33702 

12 

20 

.78 

12541 

14397 

16232 

18106 

19962 

21817 

23672 

25527 

27383 

29238 

31093 

32948 

34803 

14 

20 

.04 

16985 

19309 

21634 

23958 

26282 

28636 

30930 

33255 

35579 

37903 

40227 

42551 

44876 

14 

22 

.47 

17166 

19621 

22J76 

24530 

26992 

29448 

319J4 

34359 

36815 

39270 

41726 

44182 

46637 

14 

24 

.94 

16955 

19509 

22064 

24619 

27173 

29/27 

32284 

34839 

37393 

39948 

42508 

45063 

47618 

16 

24 

.25 

22385 

25514 

28642 

31771 

34899 

38027 

41149 

44277 

47405 

50532 

53660 

56787 

59915 

16 

26 

.64 

22378 

25638 

28900 

32159 

35419 

38679 

41939 

45200 

48460 

51720 

54980 

58241 

61500 

18 

26 

.09 

28157 

32028 

35900 

39772 

43645 

47516 

51388 

55260 

59132 

63004 

66876 

70748 

74620 

18 

30 

.78 

28209 

32J83 

36557 

407S1 

44905 

49079 

53253 

57427 

61601 

65775 

69949 

74123 

78298 

20 

30 

.25 

34939 

39856 

44743 

49638 

54517 

59404 

64291 

69178 

74065 

78952 

83838 

88725 

93613 

22 

36 

.67 

42280 

48459 

54639 

60818 

66998 

73178 

79357 

85537 

91716 

97896 

104076 

110255 

116435 

24 

36 

.25 

50357 

57394 

64431 

71469 

78506 

83544 

9258! 

99619 

106656 

113694 

120731 

134806 

26 

42 

.61 

59129 

67714 

76298 

84882 

93466 

102050 

110634 

119218 

127802 

136..8/ 

144971 

153555 

162139 

282 


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A-        1 

Types  of  Compound  Pumps 

Compound  pumps  are  built  with  the  high-pressure  steam 
cylinder  outboard,  as  shown  in  figure  117  or  with  the  low  pressure 
steam  cylinder  outboard,  as  shown  in  figure  118.  The  latter 
type,  which  is  known  as  a  three-rod  pattern  compound  is  par- 
ticularly desirable,  on  account  of  the  accessibility  of  the  pistons 
and  rods. 


Fig.  117- 
Compound  Piston  Pump. 


Fig.  118 
Compound  Center-Packed  Plunger  Pump. 


AND    CONDENSERS  "FOR   EVERT  SERVICE         B) 

,BHB^^BBBBHB,^HtfBB,,Byl,H,,,,I,HBBBtf,,^Biil.B,,,B,^^B<,i.iU^I»i»B..WW».lfi\ 

283 


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OMPANY 

Suction 


Suction  is  a  term  used  to  denote  a  vacuum,  since  suction 
cannot  be  produced  without  removing  the  atmospheric  pressure. 
Elevating  water  by  suction  is  raising  water  by  means  of  or 
through  the  agency  of  a  vacuum.  Simply  creating  a  vacuum, 
however,  will  not  enable  water  to  be  raised.  A  vacuum  in 
itself  is  not  capable  of  raising  water.  We  must  have  pressure 
to  raise  or  force  the  water  up,  and  this  pressure  must  be  ap- 
.  plied  on  the  opposite  side  of  the  water  to  be  raised  to  the  space 
in  which  the  vacuum  is  created.  This  is  illustrated  in  figure  119. 


Fig.  119 
Sketch  illustrating  how  water  is  raised  by  suction. 

We  have  an  air  tight  tank  A  containing  a  quantity  of 
water.  To  this  tank  are  connected  two  pumps  D  and  E,  the 
suction  pipe  of  D  being  submerged,  and  the  suction  pipe  of  E 
not  submerged.  If  the  pump  E  is  started,  a  vacuum  will  be 
created  in  the  tank  A  above  the  water,  and  the  water  will  be  in 
a  vacuum.  The  pump  cannot  raise  the  water,  because  there  is 
no  pressure  to  raise  it  to  the  pump.  If  valve  B  in  the  top  of  the 
tank  is  opened,  air  will  be  admitted,  and  the  vacuum  will  be 
broken.  This  will  have  no  effect  upon  the  water.  Assume 
now  that  we  stop  the  pump  E  and  start  the  pump  D  with  the 
valve  B  open.  A  vacuum  is  created  in  the  suction  pipe  of 
pump  D  above  the  water,  and  the  pressure  on  the  surface  of  the 
water  in  the  tank  will  force  the  water  up  in  the  pipe  of  the  pump. 


284 


B  A  T  T  L  E      C  RL  E  E  K .     MIC  HI  G  AN,      U.  S .  A. 


These  are  the  principles  involved  in  lifting  water  by  suc- 
tion. In  figure  120  is  illustrated  a  direct  acting  pump  cylinder 
and  suction  pipe.  As  soon  as  the  pump  removes  a  portion  of 
the  air  pressure  inside  the  pipe,  the  pressure  inside  and  outside 
will  be  unbalanced.  As  water  under  pressure  presses  equally 
in  all  directions,  if  the  resistance  be  removed  at  any  point,  the 
water  will  flow  in  that  direction,  being  forced  along  or  upward 
by  reason  of  the  unbalanced  pressures.  In  other  words,  when 
a  partial  vacuum  is  created  in  the  suction  pipe,  the  pressure 
or  resistance  at  this  point  is  decreased,  and  the  pressure  on  the 
same  area  of  water  outside  the  pipe  is,  therefore,  the  greatest, 
and  the  water  is  forced  up  in  the  pipe. 


Fig.  120. 
Sketch  Showing  Fluid  Cylinder  and  the  Course  of  Fluid 

Through  Same. 

The  distance  or  height  to  which  water  will  be  forced  up 
in  the  pipe  depends  upon  how  much,  or  to  what  extent  the 
resistance  or  pressure  has  been  removed.  A  column  of  water  1  * 
square,  and  27.6"  high,  weighs  1  Ib.  If  the  pressure  on  each 
square  inch  of  the  surface  of  the  water  in  the  pipe  be  reduced 


285 


1  lb.,  the  water  will  rise  27.6*  in  the  pipe.  If  2  Ibs.  pressure 
be  removed,  it  will  rise  twice  as  high  or  55.2",  and  so  on.  Now 
the  pressure  on  the  outside  of  the  pipe,  i.e.,  the  air  pressure 
down  on  the  surface  of  the  water,  is  merely  the  weight  or  pressure 
of  the  atmosphere,  which  at  sea  level  is  14.7  Ibs.  on  each  square 
inch.  It  will  be  seen,  therefore,  that  there  is  a  limit  to  the 
height  to  which  the  water  may  be  raised  by  suction,  or  atmos- 
pheric pressure.  The  maximum  theoretical  .  height  is  equal  to 
14.7X27.6'',  which  is  405.72",  or  33.83  feet.  Owing  to  leakage 
of  air  and  frictional  losses,  this  height  is  reduced  to  26  feet  in 
practice. 

The  curve  below  gives  the  theoretical  and  practical 
suction  lift  of  water  at  various  temperatures  at  sea  level. 
The  upper  curve  gives  the  maximum  possible  suction  lift,  and 
the  lower  curve  is  the  practical  suction  lift. 


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286 


Suction  at  Altitudes 

For  altitudes  above  sea  level  where  the  barometric  pressure 
is  less  than  14.7  Ibs.  per  square  inch,  the  water  suction  lift  is 
less  than  at  sea  level.  A  pump  that  will  raise  water  26  feet  at 
sea  level  would  only  raise  it  21.4  feet  if  placed  at  an  altitude  of 
one  mile.  The  following  table  gives  the  maximum  lift  possible 
for  different  altitudes. 

SUCTION  LIFT  AT  DIFFERENT  ALTITUDES 


Miles 

Feet 

Theo.  Lift. 

Actual  Lift. 

Sea  Level 

X 

0 
1,320 

33.83 
32.38 

26 
24.9 

2,556 

30.79 

23.7 

% 

3,960 

29.24 

22.5 

I 

5,280 

27.76 

21.4 

iM 

6,600 

26.38 

20.3 

7,836 

25.13 

19.3 

2 

10,560 

22.82 

17.5 

Handling  Hot  Water  and  Other  Liquids 

By  referring  to  figure  121,  it  will  be  seen  that  for  handling 
hot  water  168°  and  above,  it  is  necessary  that  the  water  should 
flow  to  the  pump.  Boiler  feed  pumps  are  generally  placed 
below  the  feed  water  heater,  so  that  the  water  flows  to  them 
under  a  head  of  5  to  10  feet,  depending  upon  the  temperature 
of  the  feed  water. 

For  pumping  liquids  other  than  water,  the  suction  lift 
possible  depends  on  the  specific  gravity  of  the  liquids.  Thick 
liquids,  such  as  tar,  molasses,  should  always  flow  to  the  pump 
by  gravity,  or  under  a  head. 

The  Suction  Pipe 

It  is  always  desirable  to  place  a  pump  as  near  the  source  of 
supply  as  possible.  While  it  requires  no  more  power  to  raise 
water  by  suction  than  to  discharge  it  an  equal  distance,  the 
disadvantage  of  the  long  suction  line  is  that  a  very  small  leak 
under  a  high  vacuum  is  likely  to  disable  the  pump,  while  a  leak 
several  times  the  size  in  the  discharge  line  would  not  affect  the 
pump.  Furthermore,  owing  to  the  larger  size  of  the  suction 
line,  a  long  line  adds  to  the  cost  of  the  installation. 


287 


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The  height  of  lift  is  always  measured  vertically  between 
the  surface  of  the  water,  and  the  center  of  the  suction  inlet  at 
the  pump.  If  the  water  level  is  liable  to  fluctuate,  the  height 
at  which  the  pump  is  placed  above  the  water  is  reckoned  from 
the  lowest  water  level. 

With  long  suction  lines,  the  friction  loss  should  be  taken 
into  consideration,  when  calculating  the  suction  lift. 

When  a  pump  is  to  operate  on  a  suction »lift  of  15  feet  or 
more,  it  is  advisable  to  install  a  foot  valve  on  the  suction  pipe 
in  order  to  insure  a  smooth  operation  of  the  pump.  The  object 
of  a  foot  valve  is  to  keep  the  pump  primed,  and  it  allows  the 
pump  to  start  off  easily,  without  having  to  fill  the  suction 
pipe  at  each  stroke. 

In  freezing  weather,  provision  must  be  made  for  draining 
the  suction  pipe  and  water  cylinder. 

The  suction  pipe  should  be  carefully  laid,  and  all  joints 
made  tight.  The  suction  line  should  be  securely  suspended  to 
avoid  any  vibration,  which  might  cause  a  leak.  Where  the 
suction  pipe  is  very  long,  or  the  lift  high,  a  suction  air  chamber 
on  the  suction  pipe  assists  the  pump  in  starting  the  long  column 
of  water  at  each  stroke,  and  it  also  stops  the  motion  of  the  water 
without  shock,  in  case  the  pump  is  operated  at  high  speed. 
Suction  air  chambers  are  preferably  placed  as  shown  in  figure 
122. 

Size  of  Suction  and  Discharge  Pipes 

If  the  speed  of  the  wacer  in  the  suction  pipe  were  to  be 
kept  the  same  as  the  speed  of  the  pump  piston  or  plunger,  the 
sucticn  pipe  of  course  would  have  to  be  the  same  size  as  the 
water  cylinder.  While  this  would  represent  an  ideal  condition 
as  far  as  friction  is  concerned,  it  would  also  mean  a  very  large 
suction  pipe,  and  an  unnecessary  added  expense.  It  is  con- 
sidered good  practice  to  strike  a  mean  between  the  loss  by 
water  friction  and  the  use  of  an  exceptionally  large  suction  pipe. 
In  doing  this  it  has  been  found  from  experience  that  a  velocity  of 
approximately  250  feet  per  minute  in  the  suction  pipe  will  give 
good  results.  The  area  of  the  suction  pipe,  therefore,  will  be 
as  much  smaller  than  the  area  of  the  cylinder,  as  the  piston 
speed  is  less  than  250  feet  per  minute.  If  the  piston  speed  was 
100  feet  per  minute,  then  the  area  of  the  suction  pipe  would 
be  40%  of  the  area  of  the  water  cylinder,  or  cylinders.  In 


288 


BATTLE      CREEK       M  I C  H  I  G  AN . 


other  words,  the  area  of  the  suction  pipe  in  square  inches  is 
equal  to  the  area  of  the  water  piston  times  the  piston  speed  in 
feet  per  minute,  divided  by  250. 

Example 

Calculate  the  size  of  the  suction  pipe  for  a  12X8X12 
simplex  pump  based  on  the  pump  making  100  strokes  per 
minute,  or  100  feet  piston  travel. 

Solution 

The  area  of  the  water  cylinder  or  piston  is  50.26  square 
inches,  and  the  piston  speed  in  feet  per  minute  is  100.  The 
area  of  the  suction  pipe  will  then  be 

50X100 

— rrr =  20.1  Square  inches. 

which  corresponds  to  a  diameter  of  about  5". 

The  size  of  the  discharge  pipe  may  be  calculated  in  the  same 
manner  by  using  a  velocity  of  400  feet  per  minute  through  the 
discharge  pipe,  instead  of  250  feet. 

Example 

Calculate  the  size  of  the  discharge  pipe  for  a  12x8x12  pump 
based  on  the  pump  making  100  strokes  per  minute  or  100  feet 
piston  travel. 

Solution 

The  area  of  the  8"  water  cylinder  or  piston  is  50.26  square 
inches,  and  the  piston  speed  in  feet  per  minute  is  100.  The  area 
of  the  discharge  pipe  will  then  be 

50.26X100 

=  12.56  Square  inches. 

400 

which  corresponds  to  a  diameter  of  4  ". 

Assuming  a  practical  velocity  of  water  in  the  suction  pipe 
of  250  feet  per  minute,  and  a  velocity  in  the  discharge  pipe  of 
400  feet  per  minute,  the  sizes  of  suction  and  discharge  pipes 
may  be  calculated  from  the  following  formulae: 

(48) 
(49) 
In  which  Dt  =  Diameter  of  suction  pipe. 

D2  =  Diameter  of  discharge  pipe. 

G  =  Gallons  per  minute. 


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289 


Fig.  122 
Sketch  Showing  Proper  Location  of  Suction  Air  Chamber. 

Air  Chambers 

Air  chambers  are  generally  of  cast  iron,  and  may  be  attached 
to  the  discharge  pipe  or  to  the  suction  pipe.  When  the  air 
chamber  is  attached  to  the  discharge  pipe,  it  is  called  a  discharge 
air  chamber,  and  when  attached  to  the  suction  pipe,  it  is  called 
a  suction  air  chamber.  The  object  of  an  air  chamber  is  to  pro- 
vide an  elastic  element  in  the  pipe  line  to  take  up  the  shocks 
and  pulsations,  and  produce  a  uniform  flow  in  the  pipe.  The 
discharge  air  chambers  are  generally  furnished  on  simplex  pumps 
of  all  kinds,  except  those  used  for  vacuum  service.  The  dis- 
charge air  chambers  are  not  furnished  on  the  smaller  sizes  of 
duplex  pumps.  However  they  are  advisable  on  larger  sizes. 

Discharge  air  chambers  are  generally  provided  with  an 
opening  on  the  side  near  the  top  for  charging  with  air.  How- 
ever if  there  is  not  a  supply  of  compressed  air  available,  a  snifting 
valve  of  pet  cock  may  be  placed  in  the  suction,  which  will  admit 
sufficient  air  to  the  water  to  properly  charge  the  air  chamber. 


290 


Where  the  suction  pipe  is  very  long,  or  the  suction  lift  high, 
an  air  chamber  on  the  suction  pipe  is  recommended,  as  it  as- 
sists the  pump  in  starting  the  long  column  of  water  at  each  stroke, 
and  it  also  stops  the  motion  of  the  water  without  shock,  in  case 
the  pump  is  operated  at  high  speed.  Suction  air  chambers 
should  be  placed  as  shown  in  figure  122,  and  the  capacity  of  the 
suction  air  chamber  should  be  approximately  6  to  8  times  the 
capacity  of  the  water  cylinder. 


GHtHk* 


Fig.  123 

Sketch  Showing  Arrangement  of  Piping  on  Water  End  to  Determine 
the  Total  Head. 


c 

AND 

CONDEN 

S 

ERS 

FOR 

EVERV 

SERVICE         |] 

291 


J- 

u 

N 

10 

N 

S 

TE 

AM 

P 

UM 

P 

COMPANY     Z| 

Measurement  of  Total  Head 

The  total  head  of  a  pump  may  be  found  by  a  test  gauge 
placed  on  the  discharge  pipe,  and  to  its  reading  must  be  added 
'the  distance  from  the  center  of  the  gauge  to  the  level  of  the 
water  in  the  suction  well  (see  figure  123).  If  the  suction  pipe 
is  long,  the  suction  lift  may  be  found  by  placing  the  vacuum 
gauge  on  the  suction  pipe  close  to  the  pump.  The  readings  of 
the  two  gauges  are  added,  as  is  also  the  distance  between  the 
center  of  the  discharge  gauge,  and  the  point  where  the  vacuum 
gauge  is  attached. 

In  case  the  water  flows  to  the  pump  under  a  head,  this 
amount  should  be  deducted  from,  the  reading  of  the  discharge 
gauge  to  arrive  at  the  total  head. 

The  velocity  head  in  direct  acting  pumps  is  generally  neg- 
ligible, as  the  velocities  are  low. 

Performance  Factors 

Speeds 

The  normal  speed  a  pump  should  run  depends  upon  the 
size  of  the  pump  and  the  conditions  of  service. 

For  boiler  feed  service,  where  hot  water  is  handled,  the  pump 
must  run  at  slow  speeds  25  to  35  strokes  per  minute,  for  best 
results. 

The  following  table  gives  the  approximate  piston  speeds 
of  direct  acting  pumps  for  different  conditions  of  service. 

Piston  Speeds  for  Pumps 


0. 

6 

3 

Piston  or  Plunger 
Pumps  handling 
Cold  Water 

Sorter  Feed  Pumps 
Thick  Liquor 

Wet  Vacuum 
Pumps 

Piston,  Plunger  or 
Hydraulic  Pressure 
Pumps 

h 

Pumps 

"o 
o 
M 

100  pounds  pressure 
and    under 

Pumps  handling 
Hot    Wat.r 

Jet   Condensers 

Handling  Cold 
Water  150  Pounds 
Pressure  or  over 

2 

& 

Strokes 

Feet 

Strokes 

Fe°t 

Strok-s 

Feet 

Strokes 

Feet 

per  Min. 

per  Min. 

per  Min. 

per  Min. 

per  Min 

per  Min. 

per  Min. 

per  Min. 

3 

150 

37.5 

60 

15 

100 

25 

100 

25 

4 

150 

50 

60 

20 

100 

33.3 

100 

33.3 

5 

140 

58.5 

58 

24.2 

100 

41.6 

90 

37.5 

6 

125 

62.5 

55 

27.5 

100 

50 

85 

42.5 

7 

120 

70 

55 

32 

100 

58.3 

85 

49.6 

8 

112 

74.6 

50 

33.3 

100 

66.7 

80 

53.3 

10 

100 

83.3 

42 

35 

100 

83.3 

75 

62.5 

12 

90 

90 

35 

35 

100 

100 

75 

75 

16 

75 

100 

35 

46.7 

75 

100 

60 

80 

20 

60 

100 

30 

50 

60 

100 

54 

90 

24 

50 

100 

25 

50 

50 

100 

45 

90 

For  cold  water  service  against  low  pressures,  100  pounds 
and  under,  piston  speeds  up  to  100  feet  per  minute  depending 
upon  the  size  of  the  pump,  can  be  successfully  used. 

For  high  pressure  service,  150  pounds  and  over,  pumps  are 
generally  operated  at  moderate  speed. 

Pumps  handling  thick  liquids  like  syrup,  molasses,  heavy 
oil,  etc.,  which  cannot  be  made  to  flow  fast  should  also  run  slow. 

Displacement 

The  displacement  of  a  single  double  acting  pump  can  be 
calculated  theoretically  by  the  following  formula: 

AXTX12 
D  =  -  -  .  0408d2T 

231  (50) 

In  which  D  =  Displacement  of  double  acting  plunger,  U.  S. 
gallons  per  minute. 

A  =  Area  of  piston  or  plunger  in  square  inches. 

d=  Diameter  of  piston  or  plunger. 

T=  Piston  travel  in  feet  per  minute. 

If  it  is  desired  to  find  the  diameter  of  the  water  piston  or 
plunger  to  give  a  specified  displacement,  formula  51  may  be  used. 

~D~  (51) 


In  which  d  =  Diameter  of  the  piston  or  plunger. 
D  =  Displacement  in  U.  S.  gallons  per  minute. 
T  =  Piston  travel  in  feet  per  minute. 

Example 

Assume  we  wish  to  find  the  diameter  of  a  pump  piston  to 
handle  SOO  gallons  per  minute  at  75  feet  piston  travel.  Sub- 
stituting in  formula  51. 

SOO 
d=4.95 


ISOO 
\~75~ 


75 

=4.95X3.26 
=  16.13" 

Therefore  use  a  16"  piston. 

In  the  center  packed  plunger,  or  the  piston  pump,  the 
displacement  of  the  piston  rod  must  be  deducted,  if  accurate 
results  are  desired. 


I 


AND  ^^p^B^SERSFOR_^VB^_SEKy_lC  E 

293 


UNION       STEAM       PUMP       COMPANY 


Slip 

There  is  a  loss  of  capacity  in  the  operation  of  a  pump  due 
to  leaky  valves,  piston  packing,  stuffing  boxes,  or  suction.  This 
loss  is  generally  stated  as  a  percentage  of  the  displacement, 
and  is  called  the  slip. 

SUP  -          (62) 


In  which  L  =  Loss  by  leakage  in  gallons  per  minute. 
D  =  Displacement  in  gallons  per  minute. 

Slip  varies  in  pumps  from  2%  to  10%,  depending  entirely 
upon  the  condition  of  the  pump.  It  is  customary  to  use  a  figure 
of  5%  in  estimating  the  slip  of  a  pump. 

Capacity 

The  capacity  of  a  pump  is  the  actual  volume  of  liquid 
delivered,  and  equals  the  displacement  minus  the  slip. 

C  =  D—  S  (53) 

In  which  C  =  Capacity  in  gallons  per  minute. 

D  =  Displacement  in  gallons  per  minute. 

S  =Slip  in  gallons  per  minute. 

The  capacity  of  a  pump  may  be  found  by  calculation, 
assuming  a  factor  for  the  slip,  or  by  actually  measuring  the 
water  by  weir,  tank,  nozzle,  or  pitot  tube,  as  described  on 
page  110. 

In  calculating  the  displacement,  or  capacity  of  a  pump  by 
the  formula  given,  the  results  obtained  are  in  U.  S.  gallons  of 
231  cubic  inches. 

In  Great  Britain,  and  her  colonies,  the  Imperial  gallon  is 
used,  which  contains  277  cubic  inches,  or  is  20%  larger  than  the 
U.  S.  gallon. 

Volumetric  Efficiency 

The  volumetric  efficiency  of  a  pump  is  the  ratio  of  the 
capacity  to  the  displacement,  and  equals 

C  (64) 

Ev=rT 


BATTLE      CREEK.     MICHIGAN,      U.  S.  A. 


Hydraulic  Efficiency 

The  hydraulic  efficiency  is  the  ratio  of  the  total  head  pumped 
against  to  the  total  head  pumped  against  plus  the  hydraulic  losses, 
equals 


(66) 


The  hydraulic  losses  consist  of  the  frictional  losses,  in  the 
suction  pipe,  through  the  pump  valves,  and  seats,  as  well  as  the 
velocity  head. 

Mechanical  Efficiency 

The  ratio  of  the  indicated  horse  power  of  the  water  end  to 
the  indicated  horse  power  of  the  steam  end  is  the  mechanical 
efficiency,  and  equals 


(56) 


The  mechanical  efficiency  of  direct  acting  pumps  varies 
with  the  size  and  type  from  50%  to  90%.  This  factor  can  be 
determined  only  by  actual  test. 

The  following  table  gives  an  approximate  idea  of  the  mechan- 
ical efficiency  of  direct  acting  pumps  of  the  piston  and  outside 
packed  types. 

In  calculating  pump  sizes,  to  take  care  of  any  possible 
drop  in  steam  pressure,  or  unforeseen  conditions,  we  recommend 
that  the  mechanical  efficiency  be  taken  at  80%  of  the  values 
given  in  the  following  table. 

MECHANICAL  EFFICIENCY  PERCENT 


Stroke 

Piston 

Outside  Packed 

of  Pump 
Inches 

Type  Percent 

Plunger  Type 
Percent 

3 

55 

50 

5 

60 

56 

6 

65 

61 

7 

68 

64 

8 

72 

68 

10 

76 

72 

12 

78 

75 

16 

80 

77 

20 

83 

80 

24 

85 

82 

AND    CO N"D ENS E  R  S    F  O  R   EVERT  SERVICE 


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Overall  Efficiency 

This  efficiency  comprises  all  losses  in  the  pipe,  and  indi- 
cates the  economy  of  the  whole  unit.     It  is  expressed  as  follows : 

E0=EhyXEvxEm  (67) 

Steam  Indicated  Horse  Power 

The  steam  indicated  horse  power  of  a  pump  is  calculated 
by  the  formula 

P.  L.  A.  N.  (68) 

Horse  Power  =  - 


P  =  Indicated  M.  E.  P.  pounds  per  square  inch. 
L=  Length  of  stroke  in  feet. 
A  =  Area  of  steam  piston  in  square  inches. 
N  =  Number  of  strokes  per  minute. 

Water  Horse  Power 
The  horse  power  of  the  water  end  equals. 


H    PW=  =  .000252G.H. 

33000  (59) 

Where  G=U.  S.  Gallon's  per  minute  delivered. 

W=  Weight  of  one  U.  S.  gallon  in  pounds. 
H  =  Total  head  pumped  against  in  feet. 
Example 

Find  the  water  horse  power  of  a  pump  delivering  500  U.  S. 
gallons  per  minute  against  a  head  of  200  Ibs. 

Solution 
lib  =2.31  feet. 
200  Ibs  -200X2.31  =462  feet. 
Now  substituting  in  formula  59, 
H   P    =  .  000252X500X462  =58.2 


PUMPING  " 


29G 


Materials  and  Manner  of  Fitting  Pumps  for  Hand- 
ling Different  Liquids  and  Gases 

Direct  acting  pumps,  power  pumps,  and  crank  and  flywheel 
pumps  are  classified  according  to  the  manner  in  which  the 
liquid  cylinder  is  fitted,  as  follows : 

Standard  Fitted :  This  means  that  the  pump  is  fitted  with 
cast  iron  liquid  cylinder,  steel  piston  rod,  bronze  liner,  bronze 
valve  seats,  bolts  and  springs,  rubber  or  bronze  valves,  and  cast 
iron  liquid  piston  or  plunger. 

Standard  Bronze  Fitted :  This  signifies  a  pump  fitted  with 
cast  iron  liquid  cylinder,  bronze  piston  rod,  bronze  liner,  bronze 
valve  seats,  bolts  and  springs,  rubber  or  bronze  valves,  and  cast 
iron  liquid  piston  or  plunger. 

Full  Bronze  Fitted:  This  is  a  pump,  which  carries  a  cast 
iron  liquid  cylinder,  bronze  liner,  bronze  valve  seats,  bolts  and 
springs,  rubber  or  bronze  valves,  bronze  liquid  piston  or  plunger. 

All  Iron  Fitted :  Pumps  for  handling  tar,  ammonia,  etc.  are 
built  without  bronze  fittings.  In  this  type  of  pump  the  liquid 
cylinder  is  of  cast  iron,  the  piston  rod  is  of  steel,  valve  seats 
and  valves  of  cast  iron,  valve  bolts  of  steel,  valve  springs  of 
steel,  and  liquid  piston  or  plunger  of  cast  iron.  Iron  fitted 
pumps  are  furnished  with,  or  without  cast  iron  liners,  depending 
on  the  size  of  the  pump. 

All  Bronze:  This  is  a  pump  with  the  liquid  cylinder  of 
bronze,  bronze  liner,  bronze  piston  rod,  bronze  valve  seats,  bolts 
and  springs,  bronze  valves  and  bronze  water  piston  or  plunger. 

In  the  above  classification,  the  term  "Standard  Fitted" 
generally  applies  to  duplex  pumps  only.  Simplex  Pumps  are 
built  regularly,  "Standard  Bronze  Fitted." 

The  following  list  gives  an  idea  of  the  proper  fitting  foi 
pumps  for  handling  different  liquids,  as  well  as  the  type  of  liquid 
valve  to  use,  and  the  kind  of  packing  in  the  liquid  piston  or 
plunger. 


jji        AND    CONDENSERS 

-FOR 

EVERV 

5 

ERVICE 

3 

297 


The  Materials  and  Fittings  Used  for  Pumping 
Various  Liquids 

Direct  Acting  Pumps,  Power  Pumps  Crank  and  Flywheel 

Pumps 


The  following  table  gives  the  proper  materials  and  fittings  to  be  used  on  pumps  for 
handling  different  kinds  of  liquids. 


Kind  of  Liquid 

Material  Used 

Valves 

Piston  Pack    g 

Acetic  Acid  Concentrated 

All  Bronze 

Bronze  disc 

Hydraulic 

Acetic  Acid  Diluted 

All  Bronze 

Bronze  disc 

Hydraulic 

Acid  Mine  Water 

All  Bronze 

Bronze  disc 

Hydraulic 

Alkaline  Water 

All  Iron  Fitted 

Iron  disc 

Hydraulic 

Alcohol  (crude) 

Standard  Bronze  fitted 

Bronze  disc 

Hemp 

Ammonia  Water(Aqua  Am.) 
Anilin  Water 

All  Iron  fitted 
All  Iron  fitted 

Iron  disc 
Iron  disc 

Hydraulic 
Hydraulic 

Benzene 

All  Iron  fitted 

Iron  disc 

Hemp 

Benzine 

Standard  Bronze  fitted 

Bronze  disc 

Hemp 

Beer 

All  Bronze  fitted 

Bronze  disc 

Hydraulic 

Beer-wort 

All  Bronze  fitted 

Bronze  disc 

Hydraulic 

Beet  Juice  (thin) 

All  Iron  fitted 

Iron  disc 

Hydraulic 

Bisulphite 

Standard  Bronze  fitted 

Bronze  disc 

Hemp 

Bitter  Mineral  Water 

All  Bronze 

Bronze  disc 

Hydraulic 

Brine  (Calcium) 

All  Iron  fitted 

Iron  disc  or 

rubber 

Hydraulic 

Brine  (Sodium) 

Standard  Bronze  fitted 

Bronze  disc  or 

rubber 

Hydraulic 

Cane  Juice 

Full  Bronze  fitted 

Bronze  disc 

Hydraulic 

Carbonate  of  Soda 

All  Iron  fitted 

[ron  disc 

Hydraulic 

Carbonic  Acid 

Standard  Bronze  fitted 

Bronze  disc 

[ron  Ring 

Caustic  Carbonate  of  Soda  in 

Solution  (Hot) 

All  Iron  fitted 

Iron  disc 

Hemp 

Caustic  Chloride  of  Magnesium 

Solution  (Cold) 

All  Iron  fitted 

[ron  disc 

Hemp 

Caustic  Cyanogen  in  Solution 
Caustic  Manganese  in  Solution 

All  Iron  fitted 
All  Iron  fitted 

[ron  disc 
[ron  disc 

Hemp 
Hemp 

Caustic  Potash  Solution 

All  Iron  fitted 

[ron  disc 

Hemp 

Caustic  Potash  Niter  in 

Solution 

All  Iron  fitted 

.ron  disc 

Hemp 

Caustic  Soda  Solution 

All  Iron  fitted 

iron  disc 

Hemp 

Caustic  Sodium  Chloride 

Solution 

All  Iron  fitted 

Ton  disc 

rlernp 

Caustic  Zinc  Chloride 

All  Iron  fitted 

iron  disc 

flemp 

Chlorine 

Nickel  Manganese 

or  Alloy 

Chloride  of  Potash  Solution 

All  Iron  fitted 

'ron  disc 

rlemp 

Caustic  Chloride  of  Magnesium 

Solution  (Hot) 

Hard  lead 

Coal  Tar  Oil 

All  Iron  fitted 

iron  disc 

'.ron  Ring 

Creosote  Oil 

All  Iron  fitted 

'ron  disc 

'ron  ring 

Cresol 

All  Iron  fitted 

'ron  disc 

iron  ring 

Cyanogen 

Standard  Bronze  fitted 

Bronze  disc 

lemp 

Cyanide  of  Potassium 

All  Iron  fitted 

'ron  disc 

lernp 

Distillery-wort 

All  Bronze 

Bronze  disc 

iemp 

Ferrous  Chloride 

All  Iron  fitted 

'ron  disc 

lemp 

Gasoline 

Standard  Bronze  fitted 

Iemp  or  iron 

or  standard  fitted 

Bronze  disc 

ring  packing 

Glue  (Hot) 

Full  Bronze  fitted 

Bronze  ball 

Bronze  ring 

Glycerin 

All  Bronze 

Bronze  disc 

Bronze  ring 

Grease  (Hot) 

Standard  Bronze  fitted 

Bronze  disc 

Bronze  ring 

Green  Vitriol 

All  Iron  fitted 

iron  disc 

iron  ring 

Guncotton  Brine 

All  Iron  fitted 

Ton  disc 

>on  ring 

Hot  Oil  (300    °.)  Max.  temp. 

Standard  Bronze  fitted 

Bronze  disc 

Bronze  ring 

Hot  Oil(over  300°.) 

All  Iron  fitted 

Iron  disc 

iron  ring 

Asbestos  in  pis 

;on  rod 

l 

Stuffing  box 

Heavy  Oil 

Standard  Bronze  fitted 

Bronze  disc 

Bronze  ring 

Hydrochloric  acid  in  thin 

solution 

ill  Bronze 

Bronze  disc 

Bronze  ring 

Hydrochloric  acid 

All  Bronze 

Bronze  disc 

Bronze  ring 

Iron  Pyritic  Acid 

All  Bronze 

Bronze  disc 

Bronze  ring 

Lard  (Hot) 

All  Iron  fitted 

Iron  ball  valves 

ron  ring 

PUMPING    MACHINERY,    AIR   COMPRESSORS 


298 


The  Materials  and  Fittings  Used  for  Pumping 
Various  Liquids — Continued 

Direct  Acting  Pumps,  Power   Pumps,    Crank   and  Flywheel 

Pumps 

The  following  table  gives  f.ie  proper  materials  and  fittings  to  be  used  on  pumps  for 
handling  different  kinds  of  liquids. 


Kind  of  Liquid 

Material  Used 

Valves 

Piston  Packing 

Lime  Water 

All  iron  fitted 

Iron  disc 

Hemp 

Linseed  Oil 

Standard  bronze  fitted 

Bionze  disc 

Hemp 

Lye  (Caustic) 

All  iron  fitted 

Iron  Disc 

Iron  ring 

Lye  (containing  much  salt) 

Standard  bronze  fitted 

Bronze  disc 

Hemp 

Lye  Solution  (containing  sand,) 

All  iron  fitted 

Iron  disc 

Hemp 

Mash 

All  Bronze 

Bronze  ball 

Hemp 

Milk 

All  Bronze 

Bronze  disc  or 

Solid  bronze 

clapper 

piston 

Mineral  Oil 

Standard  bronze  fitted 

Bronze  disc 

Bronze  ring 

Molasses 

Full  bronze  fitted 

Bronze  ball 

Bronze  ring  or 

Hemp 

Naphtha 

Standard  bronze  fitted 

Iron  or  Bronze 

or  Standard  fitted 

Bronze  disc 

ring 

Nitric  Acid  (Concentrated) 

Lead 

Nitric  Acid  (Diluted) 

All  iron  fitted 

Iron  disc 

Flemp 

Olive  Oil 

Standard  bronze  fitted 

Bronze,  disc 

Bronze  ring 

Paraffin  (Hot) 

Standard  bronze  fitted 

Bronze  ball 

Bronze  ring 

Petroleum 

All  iron  fitted 

Iron  ball 

[ron  ring 

Petroleum  Ether 

All  iron  fitted 

Iron  disc 

Hemp 

Pitch  (Hot) 

All  iron  fitted 

Iron  ball 

[ron  ring 

Potash  Solution 

All  iron  fitted 

Iron  disc 

Hemp 

Pulp 

Standard  bronze  fitted 

Special  bait 

vaLve  pump 

Purifying  Oil 

All  iron  fitted 

Iron  disc    ' 

[ron  ring 

Rape  Oil 

Standard  bronze  fitted 

Bronze  disc 

Bronze  ring 

Rosin  (Hot) 

All  iron  fitted 

Iron  disc 

[ron  ring 

Salt  Water 

Full  bronze  fitted 

Bronze  disc  or 

rubber 

Hydraulic 

Sea  Water 

Full  bronze  fitted 

Bronze  disc  or 

rubber 

Hydraulic 

Sewage 

Full  bronze  fitted 

Bronze  disc  or 

rubber 

Hydraulic 

Sebacic  Acid 

All  bronze 

Bronze  disc 

Hemp 

Syrup 

Standard  bronze  fitted 

Bronze  disc 

Bronze  ring 

Soap  Water 

All  iron  fitted 

Iron  disc 

Hemp 

Soda 

All  iron  fitted 

Iron  disc 

Hemp 

Sodium  Chloride  Solution 

Standard  bronze  fitted 

Bronze  disc 

Hemp 

Sodium  Sulphate 

All  iron  fitted 

Iron  disc 

Hemp 

Stearic  Acid  (Hot) 

All  bronze 

Bronze  disc 

Hemp 

Sugar  Compound 

Standard  bronze  fitted 

Bronze  disc 

Bronze  ring 

Sugar  Solution 

Standard  bronze  fitted 

Bronze  disc 

Bronze  ring 

Sulphate  of  Lime 

Standard  bronze  fitted 

Bronze  disc 

Bronze  ring 

Strontia  in  Caustic  Solution 

All  iron  fitted 

Iron  disc 

Iron  ring 

Sulphide  of  Hydrogen 

All  bronze 

Bronze  disc 

Hemp 

Sulphite  of  Sodium  (Hot) 

All  iron  fitted 

Iron  disc 

Iron  ring 

Sulphuric  Acid  Concentrated 

All  iron  fitted 

Iron  disc 

Hemp 

Su1phuric  Acid  Common 

AH  bronze 

Bronze  disc 

Bronze  ring 

Sulphurous  Acid  Concentrated 

All  bronze 

Bronze  disc 

Hemp 

Sulphurous  Acid,  Diluted 

All  bronze 

Bronze  disc 

Hemp 

Tar  (Hot) 

All  iron  fitted 

Iron  ball 

Iron  ring 

Tannic  Acid 

All  bronze 

Bronze  disc 

Hemp 

Toluol 

Standard  bronze  fitted 

Bronze  disc 

Hemp 

Turpentine  Oil 

All  iron  fitted 

Iron  disc 

Iron  ring 

Vegetable  Oil 

All  iron  fitted 

Iron  disc 

Iron  ring 

Vinegar 

All  bronze 

Bronze  disc 

Hemp 

Wine 

All  bronze 

Bronze  disc 

Bronze  ring 

Wood  Alcohol 

Standard  bronze  fitted 

Bronze  disc 

Hemp 

Water  (Hot  or  Cold) 

Standard  bronze  fitted 

Rubber  or  bronze 

disc 

Hydraulic 

Water  containing  sulphur 

Standard  bronze  fitted 

Bronze  disc 

Hydraulic 

Water  containing  some  tar 

and  ammonia 

All  iron  fitted 

Iron  disc 

Iron  ring 

Wood  Pulp 

Standard  bronze  fitted 

Special  bronze 

Ball  valve  pump 

Whisky 

All  bronze 

Bronze  disc 

Hemp 

AND   CONDENSERS  -FOR   EVERY  SERVICE 


299 


Duty 

Duty  is  the  number  of  foot  pounds  of  useful  work  done  by 
1000  pounds  of  dry  steam,  or  a  1,000,000  B.  T.  U. 

Duty  formerly  meant  the  amount  of  work  done  by  100 
pounds  of  coal,  but  owing  to  the  variation  in  the  quality  of  the 
coal,  and  the  efficiency  of  the  boiler,  this  definition  was  discarded. 
-  An  efficient  boiler  will  evaporate  ten  pounds  of  water  per 
pound  of  coal.  Therefore,  in  order  to  make  a  fair  comparison 
10X100  =  1000  pounds  of  steam  was  adopted  as  a  basis  for 
rating  the  economy  of  pumps. 

The  method  of  calculating  duty  is  as  follows  : 

Let  W  =  Number  of  pounds  of  steam  used  per  horse  power 
per  hour. 

D  =  Duty  in  foot  pounds  per  1000  pounds  of  dry  steam. 

H=  Number  horse  power  developed  per  1000  pounds  dry 
steam  per  hour. 

1000 

Then  -  =  H 
W 

Now  one  horse  power  =60  X  33000  foot  pounds  per  hour. 
Therefore  1000  pounds  dry  steam  will  deliver  H  X  60  X  33000 
foot  pounds  per  hour. 

Or  substituting   1000X60X33000  foot  pounds    per  hour. 

W 

By  definition,  the  above  expression  is  the  Duty  D.  There- 
fore writing  it  down  equal  to  D,  and  multiplying  we  have, 

_  1,980,000,000  (60) 

~~ 


This  formula  enables  one  to  readily  calculate  the  rating 
in  feed  water  or  steam  consumption,  if  the  duty  is  given,  or 
vice-versa.  Thus  a  duty  of  100  million  foot  pounds  per  1000 
pounds  of  steam  is  equivalent  to  19.8  pounds  of  steam  per 
horse  power  hour. 

The  A.  S.  M.  E.  in  1891  reported  a  standard  method  of  con- 
ducting duty,  instead  of  the  above  units  of  100  pounds  of  coal, 
or  1000  pounds  of  steam,  they  recommended  a  new  unit  based  on 
1,000,000  B.  T.  U.  furnished  by  the  boiler.  The  economy  is 
then  expressed  in  foot  pounds  of  work  done  per  1,000,000  B.T.U., 
this  unit  is  the  equivalent  of  100  pounds  of  coal  when  each  pound 
imparts  10,000  B.  T.  U.  to  the  water  in  the  boiler. 


300 


Measure  of  duty;  the  principal  data  required  for  cTetermin- 
ing  the  duty  of  a  pump  is  the  work  done,  and  the  steam  con- 
sumed in  doing  this  work. 

Capacity:  The  actual  amount  of  water  delivered  by  a 
direct  acting  pump  may  be  measured  by  pitot  tube,  calibrated 
tank,  nozzle,  or  Venturi  meter,  as  illustrated  and  described  on 
page  110.  However  as  the  displacement  pump  is  really  a  meter,  it 
is  reasonably  accurate  to  calculate  the  displacement  of  the 
plunger  and  deduct  the  piston  rod,  as  well  as  deducting  5%  to 
10%  for  slip.  The  amount  of  slip  depends  upon  the  size  of 
the  pump,  as  well  as  the  conditions  of  the  valves  and  packing. 

Head:  The  head  pumped  against  is  obtained  by  placing 
a  calibrated  pressure  gauge  on  the  discharge  pipe,  and  to  its 
reading  must  be  added  the  difference  in  the  velocity  head  in 
the  suction  and  discharge  pipes,  and  the  vertical  distance  from 
the  center  of  the  gauge  to  the  level  of  the  water  in  the  suction 
well.  See  figure  123.  If  the  suction  pipe  is  long,  a  calibrated 
vacuum  gauge  should  be  placed  on  the  suction  pipe  close  to  the 
pump.  Then  to  obtain  the  total  head,  the  readings  of  the  vac- 
uum and  discharge  gauges  are  added,  as  is  also  the  distance 
between  the  center  of  the  discharge  gauge  and  the  point  where 
the  vacuum  gauge  is  connected,  and  the  difference  in  the  velocity 
heads  in  the  suction  and  discharge  pipes.  The  velocity  head 
maybe  calculated  by  formula  22,  page  108.  If  the  suction  and 
discharge  pipes  are  the  same  size,  the  velocity  head  is  zero. 

Steam  Consumption:  To  determine  the  quantity  of  steam 
used  by  the  pump,  there  are  two  methods  employed.  The  first 
method  is  by  measuring  the  amount  of  feed  water  pumped  to 
the  boiler,  and  the  second  method  is  by  measuring  the  conden- 
sate  discharged  by  the  air  pump.  The  first  method  is  used 
where  the  steam  is  condensed  in  a  jet  condenser  in  which  the 
steam  and  injection  water  are  mixed,  and  the  second  method 
is  employed  where  a  surface  condenser  is  used. 


301 


PUMP       COM  P  ANY 


Example 

A  compound  steam  pump  pumps  3,000,000  gallons  of  water 
per  twenty-four  hours  against  a  head  of  100  pounds  per  square 
inch.  The  steam  consumption  is  40  pounds  per  water  horse 
power  per  hour.  Steam  pressure  100  pounds,  exhaust  tempera- 
ture 120°  (a)  what  is  the  duty  per  1000  pounds  of  steam? 
(b)  what  is  the  duty  per  1,000,000  B.  T.U.?  A  gallon  of  water 
weighs  8%  pounds,  and  one  pound  water  pressure  equals  a  head 
of  2.31  feet. 

Solution  (a) 

Weight  of  water  pumped  in  24  hours     3,000,000X8^ 

=  25,000,000  Ibs. 


Head  pumped  against 
Work  done  in    24  hours 


Work  done  per  hour 

Water  horsepower 

Steam  used  per  hour 

Duty  per  1000  Ibs.  of  steam 


-100X2.31  =231fcet. 
=  25,000,000X231 
=5,775,000,000 

foot  Ibs. 

5,775,000,000 

24 
=240,625,000  foot  Ibs 

240,625,000 
=33,OOOX60 

=  121.5 
=4860  Ibs. 
240,625,000 


4.86 
=49,511,300  foot  Ibs 


Solution  (b) 

Net  heat  supplied  to  pump  per  pound  of  steam. 

-1188.6—  (120-32)  =1100.6    B.T.U.(See    steam    table     in 
Appendix.) 
Total  heat  furnished  to  pump  by  boiler     =1100.6x4860. 

=5,348,916,  B.  T.  U. 

Duty  per  1,000,000  B.  T.  U.  = 

240,625,000 

-=44,993,455  foot  pounds 

O.o4o 


AIR eg MP RJE . 


302 


B 

ATTLE 

C 

RE 

E 

K. 

MIC 

HIG 

AN,      U. 

S. 

.&J 

Duty  of  Pumping  Engines 


B 

o- 

V   £ 

*"*«« 

Duty  per  1000  pounds  of  coal,  on  basis  of  evaporation 

wo 

(MM 

W,  o 

as  follows: 

•o    . 

^3  C2 

£ 

III 

9.5  to  1 

9  to  1 

8.5  to  1 

8  to  1 

7  5  to  1 

100 

19,800,000 

18  ,810  .000 

17  ,820  ,000 

16  ,830  ,000 

15  ,840  ,000 

14  ,850  ,000 

95 

20  ,842  ,105 

19  ,799  ,999 

18  ,757  ,894 

17  ,715  ,799 

16,673,684 

15  ,631  ,578 

90 

22  ,000  ,000 

20  ,900  .000 

19  ,800  ,000 

18  ,700  ,000 

17  ,600  ,000 

16,500,000 

85 

23  ,294  ,117 

22  ,029  .411 

20  ,964  ,705 

19  ,799  ,999 

18  ,635  ,293 

17  ,470  ,587 

80 

24  ,750  ,000 

23  ,512  ,500 

22  ,275  ,000 

20  ,037  ,500 

19  ,800  ,000 

18  ,562  ,500 

75 

26  ,400  ,000 

25  ,080  ,000 

23  ,760  ,000 

22  ,440  ,000 

21  ,120  ,000 

19  ,8000  ,00 

70 

28  ,285  ,714 

26,871,427 

25  ,457  ,142 

24  ,042  ,856 

22  ,628  ,571 

21  ,214  ,285 

65 

30  ,461  .538 

28  ,938  ,461 

27,415,384 

25  ,892  ,307 

24  ,369  ,230 

22,846,153 

60 

33  ,000  ,000 

31  ,350  ,000 

29  ,700  ,000 

28  ,050  ,000 

26  ,400  ,000 

24  ,750  ,000 

58 

34  ,137  ,931 

32  ,431  ,034 

30  ,724  ,137 

29  ,017  ,241 

27  ,310  ,344 

25  ,603  ,448 

56 

35  ,357  ,142 

33  ,589  ,284 

31  ,821  ,427 

30  ,053  ,570 

28,285,713 

26,517,856 

54 

36,666,666 

34  ,833  ,332 

32  ,999  ,999 

31  ,055  ,556 

29  ,222  ,222 

27  ,499  ,999 

52 

38  ,076  ,923 

36  ,173  ,076 

34  ,269  ,230 

32  ,365  ,384 

30  ,416  ,538 

28  ,557  ,692 

50 

39  ,600  ,000 

37  ,620  ,000 

35  ,640  ,000 

33  ,660  ,000 

31  ,680  ,000 

29  ,700  ,000 

49 

40  ,408  ,163 

38  ,387  ,754 

36  ,367  ,346 

34,316,938 

32  ,326  ,530 

30  ,306  ,122 

48 

41  ,250  ,000 

39  ,187  ,500 

37,125,000 

35  ,062  ,500 

33  ,000  ,000 

30  ,937  ,500 

47 

42  .127  ,659 

40  ,021  ,276 

37  ,914  ,893 

35  ,808  ,510 

33,702,127 

31  ,595  ,744 

46 

43,043,478 

40  ,891  ,304 

38  ,7^9  ,130 

36  ,586  ,956 

34  ,434  ,782 

32  ,282  ,608 

45 

44  ,000  ,000 

41  ,800  ,000 

39  ,600  ,000 

37  ,400  ,OOQ 

35  ,200  ,000 

33  ,000  ,000 

44 

45  ,000  ,000 

42  ,750  ,000 

40  ,500  ,000 

38  ,250  ,000 

36,000,000 

33,750,000! 

43 

46  ,046  ,511 

43,744,285 

41  ,441  ,959 

39,139,534 

36  ,837  ,208 

34  ,534  ,883 

42 

47  ,142  ,857 

44  ,785  ,714 

42  ,428  ,571 

40  ,071  ,428 

37  ,714  ,285 

35  ,357  ,142 

41 

48  ,292  ,682 

45  ,878  ,047 

43  ,463  ,413 

41  ,048  ,779 

38,634,145 

36,219,511 

40 

49  ,500  ,000 

47  ,025  ,000 

44  ,550  ,000 

42  ,075  ,000 

39  ,600  ,000 

37  ,125  ,000 

39 

50  ,769  ,230 

48  ,230  ,768 

4o  ,692  ,307 

43  ,153  ,845 

40  ,615  ,384 

38  ,076  ,922 

38 

52  ,105  ,263 

49  ,499  ,999 

46  ,894  ,736 

44  ,289  ,473 

41  ,684  ,210 

39,978,947 

37 

53,513,513 

50  ,837  ,837 

48  ,162  ,161 

45  ,486  ,486 

42  ,810  ,810 

40  ,135  ,134 

36 

55  ,000  ,000 

52  ,250  ,003 

49  ,500  ,000 

46,750,000 

44  ,000  ,000 

41  ,250  ,000 

35 

56  ,571  ,642 

53  ,74.3  ,059 

50  ,914  ,477 

48  .085  ,895 

45  ,257  ,313 

42  ,428  ,731 

34 

58  ,235  ,294 

55  ,323  ,529 

52  ,411  ,764 

49  ,499  ,999 

46,588,235 

43  ,676  ,470 

33 

60  ,000  ,000 

57  ,000  ,000 

54  ,000  ,000 

51  ,000  ,000 

48  ,000  ,000 

45  ,000  ,000 

32 

61  ,875  ,000 

58  ,781  ,250 

55  ,687  ,500 

52  ,593  ,750 

49  ,500  ,000 

46  ,406  ,250 

31 

63  ,870  ,967 

60  ,677  ,418 

57  ,483  ,870 

54  ,290  ,321 

51  ,096  ,773 

47  ,903  ,225 

30 

66,000,000 

62  ,700  ,000 

59  ,400  ,000 

56,100,000 

52  ,800  ,000 

49  ,500  ,000 

29 

68  ,275  ,862 

64  ,861  ,968 

61  ,448  ,275 

58  ,034  ,482 

54  ,620  ,689 

51  ,206  ,896 

28 

70  ,714  ,285 

67  ,178  ,570 

63  ,642  ,850 

60  ,107  ,142 

56,157,428 

53  ,035  ,713 

27 

73  ,333  ,333 

69  ,666  ,666 

65  ,999  ,999 

62  ,333  ,333 

58  ,666  ,666 

54  ,999  ,999 

26 

76  ,153  ,846 

72  ,346  ,153 

68  ,538  ,481 

64  730  ,769 

60  ,923  ,076 

57  ,115  ,384 

25 

79  ,200  ,000 

75  ,240  ,000 

71  ,280  ,000 

67  ,320  ,000 

63  ,360  ,000 

59  ,400  ,000 

24 

82  ,500  ,000 

78  ,375  ,000 

74  ,250  ,000 

70  ,125  ,000 

66  ,000  ,000 

61  ,875  ,000 

23 

86  ,086  ,956 

81  ,782  ,608 

77  ,478  ,260 

73,173,912 

68  ,869  ,564 

64  ,565  ,217 

22 

90  ,000  ,000 

85  ,500  ,000 

81  ,000  .000 

76  ,500  ,000 

72  ,000  ,000 

67  ,500  ,000 

21 

94  ,285  ,714 

89  ,571  ,428 

84  ,857  ,142 

80  .142  ,856 

75  ,428  ,571 

70  ,714  ,285 

20 

99  ,000  ,000 

94  ,050  ,000 

89,100,000 

84,150,000 

79  ,200  ,000 

74  ,250  ,000 

19 

104  ,210  ,526 

98  ,999  ,999 

93  ,789  ,473 

88  ,578  ,947 

83  ,368  ,420 

78  ,157  ,894 

18 

110,000,000 

104  ,500  ,000 

99  ,000  ,000 

93  ,500  ,000 

88  ,000  ,000 

82  ,500  ,000 

17 

116  ,470  ,588 

110  ,647  ,048 

104  ,823  ,529 

98  ,999  ,999 

93  ,176  ,470 

87  ,352  ,941 

16 

123  ,750  ,000 

117  ,582  ,500 

111  ,375  ,000 

105  ,187  ,500 

99  ,000  ,000 

92  ,812  ,500 

15 

132  ,000  ,000 

125  ,400  000 

118  ,800  ,000 

112  ,200  ,000 

105,600,000 

99  ,000  ,000 

14 

141  ,428  .571 

134  ,357  ,142 

127  ,285  ,713 

120  ,214  ,285 

113,142,856 

106  ,071  ,428 

13 

152  ,307  ,692 

144  ,692  ,307 

137  ,076  ,922 

129,461,538 

131  ,846  ,153 

114  ,230  ,769 

12 

165  ,000  ,000 

156  ,750  ,000 

148  ,500  ,000 

140  ,250  ,000 

132  ,000  ,000 

123  ,750  ,000 

11 

180  000  ,000 

171  ,000  ,000 

162  ,000  ,000 

153  ,000  ,000 

144  ,000  ,000 

135  ,000  ,000 

10 

198  ,000  ,000 

188  ,100  ,000 

178  ,200  ,000 

168  ,300  ,000 

158  ,400  ,000 

148  ,500  ,000 

Bn    A^ 

agBaxttBBBfSSaBfSBBSBBBSBBgSSXSBBES^a  *JiA-K.v-KxxKK:x$Mxx3ntx*j£Sj. 

CONDENSERS    FOR    EVERY   SERVICE 

"I 

303 


UNION       STEAM       PUMP       COMPANY 


Table  Showing  the 
Comparative  Steam  Economy  of  Pumps 


TYPE  Weight  of  Steam 

per  1  H.  P.  per  hour 

Fly-Wheel  Triple  Expansion  condensing 13  to  16  Ibs. 

Fly-Wheel  Compound  High  Speed  with  positive  moved 

water  valve  15  to  19  Ibs. 

Fly-Wheel  Cross  Compound — regular 18  to  20  Ibs. 

Single  direct-acting  Triple  Compound  condensing — large  23  to  24  Ibs. 

Single  direct-acting  Triple  Compound  condensing— small  25  to  27  Ibs. 

Burnham  Single  direct-acting  Compound  condensing — large  30  to  33  Ibs. 

Burnham  Single  direct-act  ing  Compound  condensing — small  35  to  38  Ibs. 

Duplex  direct-acting  Triple  Compound  condensing — large  26  to  28  Ibs. 

Duplex  direct-acting  Triple  Compound  condensing — small  28  to  30  Ibs. 

Duplex  direct-acting  Compound  condensing — large 30  to  39  Ibs. 

Duplex  direct-acting  Compound  condensing — small.  ....  .40  to  43  Ibs. 

Duplex  fly-wheel  Simple  condensing — large 40  to  43  Ibs. 

Duplex  fly-wheel  Simple  condensing — small 45  to  48  Ibs. 

Duplex  fly-wheel  Simple  non-condensing — large 48  to  50  Ibs. 

Duplex  fly-wheel  Simple  non-condensing — small 52  to  55  Ibs. 

Burnham  Single  direct-acting  Compound  non -condensing 

— large 35  to  45  Ibs. 

Burnham  Single  direct-acting  Compound  non-condensing 

— small 45  to  55  Ibs . 

Duplex  direct-acting  Compound  non-condensing — large..  55  to  65*lbs. 

Duplex  direct-acting  Compound  non-condensing — small..  65  to  75  Ibs. 

Burnham  Single  direct-acting  ordinary — large 65  to  80  Ibs. 

Burnham  Single  direct-acting  ordinary — small 80  to  100  Ibs. 

Duplex  direct-acting  ordinary — large 120  to  150  Ibs. 

Duplex  direct-acting  ordinary — small 150  to  200  lb.c. 


^^ 

304 


C3 

ATT 

LE 

C 

REE 

K. 

MIC 

HIGAN. 

U. 

S. 

A. 

J| 

Capacity  of  Pumps  at  100  Feet  Piston  Speed 


*Theoretical  Capacity  of  Pumps  at  100  Feet  Speed  of  Piston  or 

Plunger 


Diameter 
of  Pump 
or  Plunger 
in  Inches 

U.  S.  Gallons  per 

Diameter 
of  Pump 
or  Plunger 
in  Inches 

U.  S.  Gallons  per 

Minute 

Hour 

24  Hours 

Minute 

Hour 

24  Hours 

1 

4.07 

244.7 

5875 

141 

828 

49704 

1192896 

U 

6.37 

382.5 

9180 

14£        858 

51648 

1235232 

If 

9.18 

550.8 

13219 

14| 

887 

53256 

1278144 

if 

12.49 

749 

17992 

15 

918 

55070 

1321915 

2 

16.31 

979 

23500 

151 

949 

56928 

1366272 

21 

20.6 

1239 

28180 

15*, 

980 

58800 

1411200 

2* 

25  5 

1530 

36720 

15f 

1012 

60720 

1457280 

2f 

30.8 

1851 

44424 

16 

1044 

62668 

1504046 

3 

36.7 

2203 

52878 

161 

1077 

64638 

1551312 

43.1 

2586 

62064 

16* 

1110 

66642 

1599408 

49.9 

2998 

71971 

16| 

1144 

68676 

1648224 

'  57.3 

3442 

82619 

17 

1179 

70752 

1698048 

4 

65.2 

3916 

94002 

171 

1214 

72840 

1748160 

41 

73.7 

4422 

106128 

17* 

1249 

74964 

1799136 

3 

82.6 

4957 

118971 

17f 

1285 

77124 

1850976 

41 

92 

5523 

132552 

18 

1322 

79314 

1903550 

5 

102 

6120 

146880 

181 

1359 

81528 

1956672 

112 

6745 

161934 

18} 

1396 

83778 

2010672 

123 

7404 

177696 

182 

•1434 

•   86060 

2065449 

134 

8093 

194248 

19 

1473 

88368 

2120832 

6 

146 

8812 

211511 

191 

1511 

90660 

2175840 

159 

9562 

229500 

19| 

1552 

93120 

2234880 

172 

10344 

248256 

19| 

1590 

95400 

2289600 

185 

11152 

267660 

20 

1632 

97920 

2350080 

7 

200 

11995 

287884 

201 

1673 

100380 

2409120 

71 
7i 

214 
229 

12867 
13769 

308808 
330478 

*4 

20$ 

1714 
1756 

102840 
105396 

2468160 
2529504 

7f 

245 

14700 

352300 

21 

1799 

107952 

2590848 

8 

261 

15667 

376011 

211 

1842 

1  10538 

2652912 

277 

16660 

399852 

21| 

1886 

113154 

2715696 

294 

17688 

424512 

2l| 

1930 

115800 

2779200 

312 

18741 

449978 

22 

1974 

118482 

2843568 

9 

330 

19828 

475887 

221 

2020 

121194 

2908656 

91 

349 

20944 

502668 

22* 

2065 

123924 

2974176 

M 

368 

22092 

530208 

22f 

2111 

126696 

3040704 

91 

388 

23280 

558720 

23 

2158 

129492 

3107808 

10 

408 

24480 

587518 

231 

2205 

132324 

3175776 

I 

428 
449 
471 

25716 
26989  ' 
28290 

617184 
647789 
678960 

1 

24 

2253 
2301 
2349 

135186 

138078 
140958 

3244464 
3313872 
3382992 

11 

493 

29616 

710784 

241 

2399 

143952 

3454848 

ii| 

516 

30986 

743677 

24J 

2449 

146958 

3526992 

lli 

539 

32374 

776993 

24| 

2499 

149952 

3598848 

111 

564 

33795 

811080 

25 

2550 

152994 

3671856 

12 

587 

35251 

846046 

25* 

2653 

159179 

3820300 

12} 

612 

36735 

881640 

26 

2758 

165484 

3971630 

12* 

637 

38250 

918000 

26* 

2865 

171908 

4125800 

12i 

663 

39816 

955584 

27" 

2974 

178457 

4282967 

13 

689 

41370 

992880 

27£ 

3085 

185130 

4443125 

131 

716 

42972 

1031328 

28 

3199 

191922 

4606125 

m 

13? 

743 
771 

44610 
46278 

1070640 
1110672 

28i 
29 

3314 
3431 

198838 
205876 

4772118 

4941028 

14 

799 

47980 

1151536 

30 

3672 

220320 

5287675 

For  duplex  pumps,  the  capacity  given  will  be  doubled. 


AND    CONDENSERS    FOR   EVERY  SERVICE 


305 


UNION       STEAM       PUMP       COMPANY 


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rH_rH_rHj-H  rH  CN  CN  _OOj*_»O  »C  CO 

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>> 

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c/5 

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Ratios  of  Areas  for  Given  Diameters  of  Steam 
and  Water  Pistons 


"0-2    VH 


DIAMETER  OF  STEAM  CYLINDERS    • 


ils 

3 

4 

4* 

5 

» 

6 

* 

7 

It 

8 

si 

10 

12 

. 

23.09 

40.93 

51.82 

64.00 

77.41 

92.16 

96.02 

125.82 

148.82 

163.84 

184.94 

256.00 

368.43 

a 

16.00 

28.44 

35.99 

44.44 

53.76 

64.00 

66.69 

87.11 

103.37 

113.77 

128.45 

177.77 

256.  00 

g 

11.75 

20.90 

26.44 

32.65 

39.49 

47.02 

48.99 

63.99 

75.93 

83.59 

94.36 

130.61 

188.10 

9.00 

16.00 

20.24 

25.  00 

30.23 

36.00 

37.50 

48.99 

58.13 

64.00 

72.24 

100.00 

144.00 

| 

7.11 

12.64 

15.99 

19.75 

23.88 

28.44 

29.63 

38.71 

45.93 

50.56 

57.08 

79.01 

113.78 

I 

5.76 

10.24 

12.95 

16.  00 

19.35 

23.04 

24.00 

31.36 

37.21 

40.96 

46.24 

64.00 

92.17 

4.76 

8.47 

10.70 

13.22 

15.99 

19.041  19.83 

25.91 

30.74 

33.85 

38.20 

52.89 

76.17 

i. 

4.00 

7.11 

8.99 

11.11 

13.44 

16.00 

16.67 

21.77 

25.84 

28.44 

32.11 

44.44 

64.00 

I 

3.40 

6.06 

7.66 

9.46 

11.45 

13.63 

14.20 

18.55 

22.01 

24.23 

27.35 

37.87 

54.54 

a 

2.93 

5.22 

6.61 

8.16 

9  87 

11.75 

12.24 

16.00 

18.09 

20.90 

23.59 

32.65 

47.02 

I 

2.5o 

4.55 

5.75 

7.11 

8.60 

10.24 

10.67 

13.93 

16.53 

18.20 

20.55 

28.44 

40.96 

2 

2.25 

4.00 

5.06 

6.25 

7.56 

9.00 

9.37 

12.25 

14.53 

1600 

18.06 

25.00 

36.00 

1.77 

3.15 

3.99 

4.93 

5.97 

7.11 

7.40 

9.67 

11.48 

12.64 

14.27 

19.75 

28.44 

1.44 

2  06 

3.23 

4.00 

4.83 

5.76 

6.00 

7.84 

9.30 

10.24 

11.56 

16.00 

23.04 

1.19 

2.11 

2.69 

3.30 

3  99 

4.76 

4.96 

6.47 

7.68 

8.46 

9.55 

13.22 

19.04 

3 

1.00 

1.77 

2.24 

2.77 

3.36 

4.00 

4.16 

5.44 

6.46 

7.11 

8.02 

11.11 

16.00 

3i 

.85 

1.51 

1.91 

2.37 

2.86 

3.40 

3.55 

4.63 

5.50 

6.06 

6.84 

9.46 

13.63 

.73 

1.30 

1.65 

2.04 

2.46 

2.93 

3.06 

4.00 

4.74 

5.22 

5.89 

8.16 

11.75 

31 

.64 

1.13 

1.44 

1.77 

2.15 

2.56 

2.66 

3.48 

.  4.13 

4,55 

5.13 

7.11 

10.24 

4 

.56 

1.00 

1.26 

1.5f 

1.89 

2.25 

2.34 

3.06 

3.63 

4.00 

4.51 

6.25 

9.00 

*J 

.49 

.88 

1.12 

1.38 

1.67 

.99 

2.07 

2.71 

3  22 

3.54 

4.00 

5.53 

7.97 

4* 

.44 

.79 

1.00 

1.23 

1.49 

.77 

1.85 

2.42 

2.87 

3.15 

3.35 

4.93 

7.11 

3 

.39 

.70 

.89 

1.10 

1.34 

.59 

1.66 

2.17 

2.57 

2.83 

3.20 

4.43 

6.38 

5 

.36 

.64 

.80 

1.00 

1.20 

.44 

1.50 

1.96 

2.32 

2.56 

2.89 

4.00 

5.76 

91 

.29 

.52 

.66 

.82 

1.00 

.19 

1.24 

1.62 

1.92 

2.11 

2.38 

3.30 

4  76 

6 

.25 

.44 

.56 

.69 

.84 

.00 

1.04 

1.36 

1.61 

1.77 

2.00 

2.77 

4.00 

''•'• 

.37 

.47 

.59 

.71 

.85 

.88 

1.15 

1.37 

1.51 

1.71 

2.37 

3.40 

7 

.33 

.41 

.51 

.61 

.73 

.76 

1.00 

1.18 

1.30 

1.47 

2.04 

2.93 

7i 

21 

.35 

.44 

.53 

.64 

.66 

.87 

1.03 

1.13 

1.28 

.77 

2.56 

8 

!25 

.31 

.39 

.47 

.56 

.58 

.76 

.90 

1.00 

1.12 

.56 

2.25 

8^~ 

28 

.34 

41 

49 

51 

67 

.80 

88 

1  00 

38 

99 

9"* 

i24 

.30 

!37 

'.44 

!46 

'.60 

.71 

.79 

.89 

.23 

.77 

9o 

.27 

.32 

.39 

.41 

.54 

.64 

70 

80 

11 

.59 

10 

30 

36 

!37 

!48 

.58 

.64 

.72 

.00 

.44 

10i 

.27 

32 

34 

44 

52 

.58 

.65 

90 

30 

ll" 

!29 

!31 

!40 

'.48 

.52 

.59 

.82 

.19 

12 

.25 

.26 

.34 

.40 

.46 

.50 

.69 

.00 

13 

28 

.34 

.37 

.42 

.59 

.85 

14 

.25 

.29 

.35 

.36 

.51 

.73 

15 

.25 

.28 

.32 

.44 

.64 

16 

.25 

.28 

.39 

.56 

17 

.25 

.34 

.49 

18 

.30 

.44 

20 

.25 

.35 

22 

.29 

24 

.24 

26 

28 

30 

3 

4 

4i 

5 

5* 

6 

* 

7 

71 

8. 

8J 

10 

12 

mrrr- 


UNION       S  T  E_AM       PUMP       COM  PANV 


Ratios    of  Areas    For  Given    Diameter  of 
and  Water  Pistons — Continued 


Steam 


DIAMETER  OF  STEAM  CYLINDERS 


Us 

14 

16 

18 

20 

22 

24 

26 

28 

30 

32 

34 

36 

501  92 

348.51 

455.11 





256  00 

334  37 

1 

196!  00 

256.00 

324.00 

400.00 

Jl 

154.87 

202.27 

256  00 

316  05 

1 

125.45 

163.86 

207.  38 

256.00 

369!  81 

I 

103.66 

135.41 

171.47 

211.39 

256.00 

J  . 

87  11 

113.77 

144  00 

177.77 

215  11 

256  66 

j  . 

74^24 

96.96 

122.72 

151.54 

183.37 

218.22 

; 

64.00 

83.59 

105.79 

130.61 

158.05 

188.  10 

226!  7i 

....... 

| 

55  75 

72.82 

92.16 

113.78 

137.67 

163.85 

192.29 

2 

49.03 

64.00 

81.00 

100.00 

121.00 

144.  OG 

1C9.00 

196.00 

225.00 

256.  GO 

38.71 

50.56 

64.00 

79.01 

95.60 

113.78 

131.56 

154.87 

177.77 

202.27 

31.36 

40.96 

51.84 

64.00 

77.44 

92.16 

108.01 

125.44 

144.00 

163.84 

'l84.'97 

....... 

25.91 

33.85 

42.84 

52.89 

64.00 

76.17 

89.39 

103.66 

119.01 

135.  41 

152.86 

3 

21.77 

28.44 

36.00 

44.44 

53.77 

64.00 

75.11 

87.11 

100.00 

113.77 

128.44 

iiiioo' 

8} 

18.56 

24.23 

30.67 

37.87 

45.83 

54.54 

64.00 

74.24 

85.22 

96.96 

109.46 

122.72 

S* 

16.00 

20.90 

26.44 

32.65 

39.42 

47.02 

55.18 

64.00 

73.47 

83.59 

94.36 

105.  79 

3f 

13.93 

18.20 

23.04 

28.44 

34.42 

40.96 

48.07 

55.75 

64.00 

72.82 

82.21 

92.16 

4 

12.25 

16.00 

20.25 

25.00 

30.25 

36.00 

42.25 

49.00 

56.25 

64.00 

72.25 

81.00 

10.85 

14.17 

17.93 

22.14 

26.79 

31.89 

37.43 

43.41 

46.51 

56.69 

64.00 

71.76 

4| 

9.67 

12.64 

16.00 

19.75 

23.90 

28.44 

33.33 

38.71 

44.44 

50.56 

57.08 

64.00 

8.68 

11.34 

14.36 

17.73 

21.45 

25.53 

29.96 

34.75 

39.89 

45.38 

51.24 

57.44 

5* 

7.84 

10.24 

12.96 

16.00 

1.19 

23.04 

27.04 

31.36 

36.00 

40.96 

46.24 

51.84 

5i 

6.47 

8.46 

10.71 

13.22 

16.00 

19.04 

22.2,3 

25.91 

29.75 

33.85 

38.21 

42.84 

6 

5.44 

7.11 

9.00 

11.11 

13.44 

16.00 

18.77 

21.77 

25.00 

28.44 

32.11 

36.00 

4.63 

6.06 

7.66 

9.46 

11.45 

13.63 

16.00 

18.56 

21.30 

24.23 

27.36 

30.67 

7 

4.00 

5.22 

6.61 

8.16 

9.87 

11.75 

13.79 

16.00 

18.37 

20.90 

23.59 

26.44 

3.48 

4.55 

5.76 

7.11 

8.60 

10.24 

12.00 

13.93 

16.00 

18.20 

20.55 

23.04 

8 

3.06 

4.00 

5.06 

6.25 

7.25 

9.00 

10.56 

12.25 

14.06 

16.00 

18.06 

20.25 

8} 

2.71 

3.54 

4.48 

5.53 

6.69 

7.97 

9.35 

10.85 

12.45 

14.17 

16.00 

17.92 

9 

2.41 

3.15 

4.00 

4.93 

5.85 

7.11 

8.34 

9.67 

11.11 

12.64 

14.27 

16.00 

2.17 

2.83 

3.59 

4.43 

5.36 

6.38 

7.49 

8.68 

9.97 

11.34 

12.88 

14.36 

10 

1.96 

2.56 

3.24 

4.03 

4.84 

5.76 

6.76 

7.84 

9.00 

10.24 

11.56 

12.96 

10i 

1.77 

2.32 

2.93 

3.62 

4.38 

5.22 

6.13 

7.11 

8.16 

9.26 

10.48 

11.75 

11 

1.62 

2.11 

2.67 

3.30 

4.00 

4.76 

5.58 

6.47 

7.43 

8.46 

9.55 

10.71 

12 

1.36 

1.77 

2.25 

2.77 

3.36 

4.00 

4.67 

5.44 

6.25 

7.11 

8.02 

9.00 

13 

1.16 

1.51 

1.91 

2.37 

2.86 

3.40 

4.00 

4.63 

5.32 

6.06 

6.83 

7.66 

14 

1.00 

1.30 

.65 

2.04 

2.46 

2.93 

3*.  44 

4.00 

4.59 

5.22 

5.89 

6.61 

15 

.87 

1.13 

.44 

1.77 

2.13 

2.56 

3.00 

3.48 

4.00 

4.55 

5.13 

5.76 

16 

.76 

1.00 

.26 

1.56 

1.89 

2.25 

2.64 

3.06 

3.51 

4.00 

4.51 

5.06 

17 

.67 

.88 

.12 

1.38 

1.67 

1.99 

2.34 

2.71 

3.11 

3.54 

4.00 

4.48 

18 

.60 

.79 

.00 

1.23 

1.49 

1.77 

2.08 

2.41 

2.77 

3.15 

3.56 

4.00 

20 

.48 

.63 

.81 

1.00 

1.21 

1.43 

1.69 

1.96 

2.25 

2.56 

2.89 

3.24 

22 

.40 

.52 

.66 

.82 

1.00 

1.18 

1.39 

1.61 

1.85 

2.11 

2.38 

2.67 

24 

.34 

.44 

.56 

.69 

.84 

1.00 

1.17 

1.36 

1.56 

1.77 

2.00 

2.25 

26 

.28 

.37 

.47 

.59 

.71 

.85 

1.00 

1.15 

1.33 

1.51 

1.71 

1.91 

28 

.24 

.32 

.41 

.51 

.61 

.73 

.86 

1.00 

1.14 

1.30 

1.47 

1.65 

30 

.28 

.35 

44 

.5$ 

.63 

.75 

.87 

1,00 

1.13 

1.28 

1.44 

14 

16 

18 

20 

22 

24 

26 

28 

30 

32 

34 

36 

308 


BATTLE      CREEK.     M I C  H  I  G  AN .      U.  S . 


1 


Valve  Area 

The  valve  area  of  a  pump,  which  is  generally  expressed  as 
a  percentage  of  the  water  piston  area,  is  the  ratio  of  the  total 
area  of  the  effective  suction  or  discharge  valves  on  one  stroke 
of  the  piston  to  the  area  of  the  water  piston.  The  valve  area 
is  generally  taken  as  the  area  through  the  valve  seat  on  the 
assumption  that  the  valve  will  lift  a  sufficient  amount,  so  that 
the  area  measured  at  the  periphery  of  the  valve  will  be  equivalent 
to  the  area  of  the  opening  in  the  valve  seat.  In  a  direct  acting 
pump,  there  is  generally  the  same  number  of  suction  valves  and 
discharge  valves,  hence,  valve  area  may  refer  to  either  suction  or 
discharge  area. 

The  valve  area  of  pumps  varies  with  the  conditions  of 
service;  vacuum  pumps,  which  handle  a  large  percent  of  air 
are  generally  given  a  valve  area  of  25  to  30  per  cent.  Boiler 
feed  pumps  generally  have  a  valve  area  of  35  to  45  per  cent. 
Pumps  operating  at  100  feet  piston  travel,  and  handling  large 
volumes  of  water  are  generally  given  a  valve  area  of  40  to  50 
per  cent.  Elevator  pumps,  which  usually  operate  at  high  speeds, 
have  a  valve  area  of  50  to  75  per  cent. 

Pump  Valves 

Direct  acting  pumps  are  generally  fitted  with  rubber  valves 
or  bro:ize  valves,  depending  on  the  service. 

Medium  rubber  valves  are  used  on  pumps  operating  on  low 
pressures  up  to  ICO  Ibs.per  square  inch  for  handling  cold  water- 


Fig.  124 

Scat  with  Rubber  Valve  and  one- 
piece  Bolt. 


Fig.  125 

Seat  with  Rubber  Valve  and  Bolt 
with  Removable  Guard 


LAND    CONDENSERS  -FOR   EVERY  SERVICE 

ffiyyyyffn TCT jnTfl^Tfy^.'^ •v^1onrT^ir?nr^Tinry^rEnJ^^  BTrgw^~E~\rir  ir^  v ..    •  >, -a-  g^v^-ysrsryTg'y^'w wV^- 


309 


UNION       STEAM       PUMP       COMPANY 


Medium  rubber  valves  are  also  used  on  wet  vacuum  pumps 
operating  on  a  high  vacuum.  Hard  rubber  valves  are  used  on 
pumps  operating  on  75  pounds  to  200  pounds  pressure  per 
square  inch,  handling  hot  or  cold  water,  and  on  vacuum  heating 
pumps.  Pumps  handling  very  hot  water  j210°  to  212°  re- 
quire special  rubber  valves,  or  bronze  valves. 

Figure  124  illustrates  the  rubber  valve  and  its  guard,  seat, 
bolt  and  spring.  The  valve  is  guided  by  the  bolt,  which  screws 
into  the  seat  on  a  taper  thread,  and  a  bronze  or  iron  guard  is 
provided  on  top  of  the  rubber  valve  in  a  bearing  for  the  spring. 
The  head  of  the  valve  bolt  provides  an  upper  guard  for  the  spring. 
This  head  may  be  cast  as  part  of  the  bolt,  as  shown  in  figure 
124  or  may  be  separate  as  shown  in  figure  126.  The  bolt  with 
the  removable  guard  is  the  type  furnished  for  hand  plate  cylinders. 
The  valve  springs  are  bronze  or  steel,  depending  on  how  the 
pump  is  fitted.  Rubber  valves  such  as  shown  in  figure  124 
can  easily  be  re -faced  when  worn. 


Fig.  126 
Seat  with  Bronze  Flat  Disc  Valve,  and  Bolt  with  Removable  Guard 

Bronze  Valves 

For  pumps  operating  on  250  to  300  pounds,  bronze  dis- 
charge valves  of  the  type  shown  in  figure  126  are  used.  This 
type  of  valve  can  be  easily  inserted  in  place  of  the  rubber  valve 
if  desired,  and  can  be  ground  to  a  good  seat. 


PUMPING    MACHINER.Y,    AIR 


310 


Fig.  127.    Bevel  Seat  Wing  Valve. 


Beveled  Seat  Wing  Valves 

For  high  pressure  pumps,  the  wing  valve  shown  in  figure 
1 27  is  used.  This  valve  has  a  conical  seat,  and  is  provided  with 
four  wings,  which  guide  the  valve  in  its  seat.  This  type  of 
valve  as  a  rule  has  a  comparatively  low  lift,  and  can  be  easily 
ground  to  a  seat  under  pressures  up  to  5000  Doundsper  square 
inch. 


Fig.  128 


Clapper 
Valve 


Clapper  Valves 

For  handling  thick  liquids,  such  as  tar,  molasses  etc.,  valves 
with  larger  opening  are  necessary.  For  this  purpose  clapper 
valves  may  be  used  (see  figure  128).  The  seat  is  generally  made 
in  the  form  of  a  rectangular  opening  in  the  valve  deck,  and  the 
valve  is  ground  to  its  seat  and  hinged. 

Ball  Valves 

The  ball  valve  is  another  and  the  more  common  type  of 
valve  used  for  handling  thick  liquids.  This  type  of  valve  gives 
a  free  opening  for  the  passage  of  the  liquid. 

The  ball  valve  illustrated  in  figure  129  consists  of  a  hollow 
ball  made  of  either  bronze  or  iron.  The  valve  seat  or  cage  may 
be  screwed  in  place  of  a  regular  valve  seat.  The  lift  of  the  ball 
valve  is  limited  by  a  cap,  which  screws  into  the  top  of  the  cage. 


AND   CONDENSERS    FOR   EVERY  SERVICE 


311 


u 

u 

N 

I  O 

N 

STE 

AM 

P 

UM 

P 

COM  PANY 

; 

Fig.  129 
Ball  Valve  and  Cage. 

Fluid  Piston  and  Plunger 

A  fluid  piston  is  generally  regarded  as  a  piston  packed  with 
either  a  fibrous  material,  or  provided  with  metallic  rings.  A 
fluid  piston  generally  works  in  a  liner,  either  of  bronze  or  iron 
depending  upon  the  service. 

The  packed  piston  is  extensively  used,  where  the  water  or 
liquid  to  be  pumped  contains  no  grit  or  sand. 

Figure  130a  shows  a  piston  packed  with  a  fibrous  material, 
such  as  is  used  on  standard  pumps. 


Fig.  130b. 

Fluid  Piston  with 

Ring-Grooved  Packing 


Fig.  130a. 
Fluid  Piston  with 
Fibrous  Packing. 


Fig.  204. 

Fluid  Piston  with 
Three-Ring  Packing. 


312 


BAT  T  L  E      C"k  EEJCl"Mi  C  H  I  G  AN . 


Metallic  Packing  and  Cup  Leather  Pistons 

For  pumps  handling  oil,  syrup  and  other  liquids,  the  piston 
is  generally  packed  with  a  solid  grooved  ring  packing  as  shown 
in  figure  130b.  This  ring  is  made  a  floating  fit  on  the  piston. 

Cup  leather  pistons,  as  illustrated  in  figure  130c  are  some- 
times used  for  handling  cold  oil  and  other  liquids. 

A  plunger  is  a  long  solid  piston  or  barrel  working  in  one  or 
two  stuffing  boxes,  which  are  packed  with  a  fibrous  material. 
Plungers  may  be  end  packed  or  center  packed  as  described  on 
pages  271-272. 

The  chief  advantage  of  the  plunger  pump  is  that  any  leakage 
by  the  plunger  may  be  eliminated,  while  the  pump  is  in  operation. 

The  plunger  pump  is  particularly  suited  for  handling  water 
or  liquids  containing  sand  and  grit,  and  also  for  pressure  pumps. 
Stuffing  Boxes 

Small  size  pumps  are  generally  furnished  with  screwed 
stuffing  boxes  as  shown  in  figure  131a.  The  customary 
type  of  stuffing  box  used  on  pumps  is  shown  in  figure  13lc 
which  has  a  bolted  gland. 

Pumps  operating  on  a  high  vacuum  require  a  water-sealed 


(b)  Fig.  131 

Sketch  Showing  Plain  Screwed  Stuffing  Box  (a);    Screwed  Type  with 
Lantern  Gland  (b);    and  Bolted  Type  (c). 


Fig.  132 
Open  Pot  Water  Seal  Stuffing  Box. 


AND    CONDENSERS    FOR    EVERY  SERVICE 


313 


UNION       STEAM       PUMP 


stuffing  box  on  the  water  end.  Two  types  are  used  for  this 
purpose,  the  ordinary  stuffing  box  with  a  lantern  gland  shown 
in  figure  131  (b)  and  the  open  pot  water  seal  shown  in  figure  132. 

Pumps  for  Different  Services 

Boiler  Feed  Pumps 

A  Committee  of  the  American  Society  of  Mechanical 
Engineers  recommended  the  unit  of  boiler  power,  known  as  the 
"Centennial  Standard",  and  this  is  now  generally  accepted. 
They  advised  that  the  commercial  horse  power  be  taken  as  an 
evaporation  of  30  pounds  of  water  per  hour  from  a  feed  water 
temperature  of  100°  of  steam  at  70  Ibs.  per  square  inch 
gauge  pressure.  This  is  practically  equivalent  to  34  >^  units 
of  evaporation,  that  is,  the  34  >£  Ibs.  of  water  evaporated  from 
a  feed-water  temperature  of  212°  into  steam  at  the  same 
temperature.  This  "Centennial  Standard"  unit  is  equivalent 
to  33,317  British  thermal  units  per  hour. 

It  was  the  opinion  of  this  committee  that  a  boiler  rated  at 
any  stated  power  should  be  capable  of  developing  that  power 
with  easy  firing,  moderate  draft,  and  ordinary  fuel,  while  ex- 
hibiting good  economy;  and  at  times  when  maximum  economy 
is  not  the  most  important  object  to  be  attained,  at  least  one 
third  more  than  its  rated  power,  to  meet  emergencies. 

In  calculating  the  size  of  a  boiler  feed  pump  it  should  be 
based  on  34>£  Ibs.  of  water  per  horse  power  per  hour,  and  should 
handle  the  rated  boiler  horse  power  when  operating  at  a  slow 
speed.  If  the  pump  is  calculated  large  enough  so  that  it  will 
operate  at  a  slow  speed,  then  in  case  of  emergency  it  can  be 
speeded  up  to  take  care  of  any  deficiencies  or  overload  that  may 
be  required  of  the  boilers. 

The  types  of  pumps  used  for  boiler  feed  service  are 
either  piston  pumps,  center  packed  plunger  pumps,  end  packed 
plunger  pumps,  or  centrifugal  pumps.  They  should  be  com- 
pound where  economy  is  essential,  or  vertical  where  floor  space 
is  limited. 

Boiler  feed  pumps  as  a  rule  exhaust  into  a  feed  water 
heater.  Thus  the  latent  heat  of  the  exhaust  steam  is  recovered, 
and  the  heat  expended  in  pumping  the  water  into  the  boilers 
amounts  to  practically  nothing. 

The  following  tables  give  the  size  of  simplex  and  duplex 
boiler  feed  pumps,  and  the  capacities  and  H.  P.  boilers  they 
are  suitable  for  at  various  speeds. 


J,,,»»iLi»jaaffia*a-""'"'"M*J"'»*a*aal''"^*^a"aj-s^^ 

f^M^rc G  'M _A C  H I N E RY^^R^£OM PR^S^S  O  RS 


314 


B 

ATT 

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C 

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EK. 

MIC 

HIGAN. 

U. 

s. 

A. 

ii 

Table  of  boiler  horse-power  capacities  of  Simplex  Pumps  at  various  speeds 
based  on  34}/£  pounds  per  horse-power  per  hour.  The  maximum,  speed  recom- 
mended for  boiler-feed  pumps  is  given  in  the  table  on  page  292. 


STROKES  PER 
MINUTE 

20 

25 

30 

35 

40 

50 

60 

Size  of  Pump 

Boile 

r  Horse-Pen 

ver  Pumps 

Will  Feed 

3    x  l^x  3 

18 

?.? 

27 

3x2x3 
4    x  2i^x  33^ 

'  '32' 

38 

23 
43 

29 
54 

35 
65 

4     x  2j^x  5 
5x3x6 
5^x  334*  7 
6^x  4x8 
7    x  4^x10 
7     x  5    xlO 
83-^x  5    xlO 
8^x  53/£xlO 
10     x  6     x!2 
10     x  63^x12 
12     x  7   -x!2 

"53 
85 
126 
200 
245 
245 
295 
425 
500 
580 

38 
66 
106 
158 
250 
308 
308 
370 
530 
685 
725 

46 
80 
126 
190 
300 
370 
370 
445 
635 
750 
870 

5i 
93 
147 
220 
350 
430 
430 
520 
745 
875 
1020 

62 

106 
168 
253 
400 
490 
490 
595 
850 
1000 
1160 

77 
132 
210 
315 
500 
6U 
615 
740 

92 
160 
253 
378 

12     x  734x12 
12     x  8     x!2 
14     x  8     x!2 
14     x  8^x12 
12     x  7     x!6 
12     x  73^x16 
12    x  8    x!6 

665 
755 
755 

850 
770 
885 
1010 

830 
945 
945 
1070 
970 
1110 
1260 

1000 
1135 
1135 
1280 
1160 
1330 
1510 

11GO 
1320 
1320 
1500 
J350 
1550 
1760 

1330 
1500 
1500 
1720 
1540 
1780 
2020 



.... 

14     x  8    x!6 
14     x  8^x16 

1010 
1140 

1260 
1420 

1510 
1710 

1760 
2000 

2020 
2280 



14     x  9     x!6 

1275 

1600 

1920 

2240 

2550 

16     xlO     x!6 

1580 

1980 

2375 

2760 

3150 

18    x!2     x!6 

2275 

2850 

3400 

4000 

4500 

20    x!4     x!6 

3100 

3875 

4650 

5400 

6200 

18     x!2     x20 

2840 

3550 

4250 

5000 

20     x!4     x20 

3850 

4820 

5800 

6750 

24     x!6     x20 

5050 

6300 

7500 

8850 

26     x!8     x20 

6400 

8000 

9600 

11200 

30     x20     x24 

9500 

11900 

14200 

16600 

Table  of  boiler  horse-power  capacities  of  Duplex  Pumps  at  various  speeds 
based  on  34J^  pounds  per  horse-power  per  hour.  The  maximum  speed  recom- 
mended for  boiler-feed  pumps  is  given  in  the  table  on  page  292. 


STROKES  PER 
MINUTE* 

20 

25 

30 

35 

40 

50 

60 

Size  of  Pump 

\          Boiler  Horse-Power  Pumps  Will  Feed 

2^x  iy2x  3 
3x2x3 
4Hx  23/^x  4 
5Mx  33^x  5 
6x4x6 
73^x  5x6 
7^x  5x8 
7^x  4^x10 
9     x  534x10 
10     x  6     xlO 
10     x  6     x!2 
10     x  7     xlO 
12     x  7     x!2 
12     x  8^x12 
14     x  83^x12 
14     xlO     x!2 
16     xlO     x!2 

23 

59 
120 
188 
290 
390 
395 
540 
700 
850 
960 
1160 
1700 
1700 
2370 
2370 

29 
74 
150 
235 
360 
490 
495 
675 
880 
1060 
1200 
1450 
2140 
2140 
2950 
2950 

20 
35 

89 
180 
280 
435 
590 
590 
810 
1060 
1270 
1450 
1740 
2560 
2560 
3550 
3550 

23 

41 
100 
210 
330 
510 
690 
690 
950 
1220 
1490 
1680 
2040 
3000 
3000 
4150 
4150 

26 
47 
118 
240 
375 
590 
785 
790 
1080 
1400 
1700 
1925 
2320 
3440 
3440 
4720 
4720 

33 

58 
148 
300 
470 
725 
985 

40 

70 
178 
360 
560 
870 
1180 

*Each  side. 


|       AND 

CONDENSERS 

FOR 

EVERY 

SERVICE          ] 

315 


L 

u 

N 

10 

N 

ST 

E  AM 

P 

UM 

P 

CO 

MPANY     l| 

Feed  Pumps  and  Receivers 

The  receiver  and  pump  is  a  desirable  outfit  for  use  in  drain- 
ing heaters,  radiators,  steam  coils  and  steam  jackets,  and  to 
force  the  water  of  condensation  in  its  hottest  condition  direct  to 
the  boilers.  This  arrangement  is  entirely  automatic  in  its  action. 
Figure  133  illustrates  the  feed  pump  and  receiver. 


Fig.  133 
Automatic  Pump  and  Receiver. 

The  condensed  steam  enters  at  the  top  and  flows  by 'gravity 
into  the  receiver,  which  is  provided  with  a  float-control  steam 
valve.  As  the  float  rises  or  falls,  the  speed  of  the  pump  is 
regulated, and  the  water  is  kept  at  a  constant  level  in  the  receiver. 

Should  it  be  desired  that  this  arrangement  be  the  sole 
means  of  feeding  the  boilers,  make-up  water  should  be  introduced 
directly  into  the  receiver  from  which  it  is  pumped  into  the  boilers. 

The  size  of  the  pump  is  calculated  on  the  basis  of  one-half 
pound  of  steam  condensed  per  hour  per  square  foot  of  direct 
radiating  surface. 

Water  Works  Pumps 

For  water  work  service,  direct  acting  pumps  of  either  the 
piston  or  plunger  pattern  are  used.  As  a  rule  a  pump  for  this 
service  is  furnished  with  a  compound  steam  end,  as  economy 
is  generally  of  prime  importance. 

Water  works  pumps  generally  are  controlled  by  a  governor, 
which  keeps  the  water  pressure  practically  constant. 


S        PUMPING    MACHINERY,    AIR   COMPRESSORS 
.li..yfutf,BUitutt,uU,...ugBt,Bai^i»uu^.^.>iltfft»iuti»it«uii. 


316 


Mine   Pumps 

For  mine  service,  two  kinds  of  pumps  are  used,  the  sinking 
pump,  and  the  station  pump. 

In  sinking  a  mine,  the  first  pump  used  is  a  sinking  pump, 
illustrated  in  figure  134,  which  is  of  the  center  packed  plunger 
type,  and  is  so  constructed  that  it  can  be  lowered  down  in  the 
mine  shaft.  It  is  secured  to  two  steel  hangers  for  hooking  over 
a  beam. 


Fig  134 

Vertu  al  Sinking  Pump. 


UNION       STEAM       PUMP       COMPANY 


1 


This  pump  is  admirably  adapted  for  this  service,  as  it  is  very 
compact,  and  the  valve  gear  and  yoke  are  entirely  enclosed, 
protecting  it  from  falling  rocks. 

When  a  desired  depth  is  reached  in  sinking  the  mine  shaft, 
a  chamber  is  cut  out,  and  a  station  pump  installed,  which  may  be 
of  the  side  plate  piston  pattern,  as  illustrated  in  figure  135,  or 
of  the  pot  valve  plunger  pattern,  as  illustrated  in  figure  109a. 

A  sump  is  provided  into  which  the  sinking  pump  delivers 
the  water,  and  the  station  pump  takes  the  water  from  the  sump , 
and  elevates  to  the  surface. 


Fig.  135 
Horizontal  Mine  Pump,  Piston  Pattern. 


Fig.  109a 
Pot  Valve  Plunger  Pump. 

Elevator  Pumps 

Direct  acting  pumps  are  used  extensively  for  supplying 
water  to  hydraulic  elevators.  These  pumps  may  be  of  either 
the  piston  or  plunger  pattern,  and  have  simple  or  compound 
steam  cylinders  depending  upon  conditions.  Figure  136  illus- 
trates a  compound  center  packed  plunger  elevator  pump. 


318 


|       BATTLE 

C 

REE 

K. 

M 

ICH 

IG 

AN. 

U. 

S. 

A. 

4 

Fig.  136 
Compound  Center-Packed  Plunger  Elevator  Pump. 


Direct  acting  pumps  are  particularly  suited  for  elevator 
service,  as  they  are  compact,  occupy  a  small  floor  space,  and 
are  ready  to  start  from  any  position  as  soon  as  steam  is  admitted 
to  the  cylinder.  They  merely  require  a  pressure  regulator  or 
governor  that  keeps  the  pressure  in  the  discharge  tank  uniform. 
Any  sudden  demand  will  lower  the  pressure  in  the  discharge  tank 
sufficiently  to  start  the  pump,  and  any  stoppage  of  the  elevator 
will  increase  the  pressure  in  the  discharge  tank  sufficiently  to 
stop  the  pump. 

Elevator  pumps  use  the  same  water  over  and  over  again, 
and  two  tanks  are  provided  for  this  purpose;  a  surge  or  succion 
tank,  and  a  compression  or  discharge  tank.  The  surge  tank 
is  generally  located  in  the  basement,  and  it  may  be  closed  or 
open.  The  discharge  tank  may  also  be  of  the  closed  or  open 
type.  If  a  closed  or  compression  tank  is  used,  the  pump  is 
controlled  by  a  pressure  regulator.  The  open  tank  is  generally 
located  in  the  roof,  and  the  pump  is  controlled  by  a  float. 

Vacuum  Pumps 

For  maintaining  vacuums  of  26 "  and  less,  the  direct  acting 
vacuum  pump  in  the  simplex  type  is  used  extensively.  Duplex 
pumps  are  not  suitable  for  vacuum  service,  as  they  short  stroke. 


AN  D    C O N D EN  S  JE RS^JFjDR^  E ,  V  E RY  S  E ,  RV I C E 

319 


There  being  no  resistance  at  the  beginning  of  the  stroke,  except 
friction,  one  piston  of  a  duplex  pump  would  move  rapidly  for- 
ward, and  throw  the  valve  of  the  opposite  pump  before  the 
piston  of  the  opposite  pump  would  have  a  chance  to  finish  its 
stroke.  The  result  would  be  a  short  stroke,  and  a  low  efficiency 
of  the  pump. 

For  these  reasons  the  simplex  pump  is  used  for  vacuum 
service.  In  this  type,  the  piston  cannot  reverse  until  it  has 
completed  its  stroke,  and  the  result  is  an  efficient  and  positive 
acting  vacuum  pump. 

Vacuum  pumps  are  divided  into  two  classes,  high  vacuum 
and  low  vacuum.  To  the  former  class  belong  those  used  for 
condensing  work  etc.,  where  a  vacuum  of  26 "  is  required,  and  to 
the  latter  class  belong  those  used  for  heating  systems  etc.,  where 
a  low  vacuum  of  10  *  to  20  "  is  required. 

High  Vacuum  Pumps 

High  vacuum  pumps,  which  have  small  clearance,  are  pro- 
vided with  soft  rubber  valves,  and  have  a  water  sealed  stuffing 
box  of  either  the  lantern  type  or  open  pot  type,  as  illustrated 
on  page  313.  This  type  of  pump  shown  in  figure  137a  is 
used  extensively  in  connection  with  jet  and  surface  condensers, 
and  vacuum  pans,  in  removing  the  air  and  condensate. 

The  method  of  calculating  the  size  vacuum  pump  to  iise 
in  connection  with  jet  and  surface  condensers  has  been  clearly 
shown  in  Section  Two  on  condensers. 


Fig.  137a 
Inverted  Suction  Valve  High  Vacuum  Pump. 


320 


BATTLE      CREEK.     MICHIGAN,     U.  S.  A. 


Fig.  137b 
Section  through  Inverted  Suction  Valve,  High  Vacuum  Pump. 

Evaporation  in  a  Vacuum 

In  sugar  factories,  as  well  as  chemical  plants  and  other 
industries,  the  modern  method  employed  for  concentrating  liquors 
is  by  boiling  them  in  a  vacuum. 

The  advantages  of  evaporating  in  a  vacuum  over  evaporating 
at  atmospheric  pressure  are,  first,  that  in  a  vacuum  all  liquids 
boil  and  evaporate  at  lower  temperatures  than  under  atmos 
pheric  pressure,  thus  there  is  a  greater  difference  in  temperature 
between  the  heating  steam,  and  the  boiling  liquid,  and  con- 
sequently a  much  greater  heat  transmission. 

Liquids  that  boil  at  high  temperatures  can  generally  not 
be  evaporated  under  atmospheric  pressure  by  means  of  high 
steam  pressure,  since  steam  would  be  required-  of  such  high 
temperatures  and  pressures,  that  its  application  would  be 
dangerous.  The  boiling  points  of  these  liquids  fall,  when 
evaporated  in  "a  vacuum,  so  that  steam  of  moderate  pressures 
may  be  used. 

The  second  advantage  of  boiling  in  a  vacuum  is  that  the 
liquid  does  not  become  as  hot  as  at  atmospheric  pressure,  and 
that  also  the  heating  surfaces,  since  steam  of  a  lower  pressure 
is  used,  are  kept  at  a  lower  temperature.  In  most  industries 
evaporating  liquids,  such  as  milk,  gelatin,  albumin  etc.,  it  is 
necessary  in  order  not  to  discolor  the  liquids,  that  they  be  evapor- 
ated at  low  temperatures. 

The  ordinary  form  of  vacuum  pan  comprises  a  spherical  or 
cylindrical  vessel,  the  lower  portion  of  which  is  steam  jacketed, 
and  fitted  with  steam  heating  coils.  At  the  upper  portion  of  the 
vessel  is  a  dome,  which  communicates  through  an  exhaust  pipe, 
provided  with  a  liquor  trap  with  a  condenser,  which  in  turn  is 
connected  with  a  vacuum  pump.  The  steam. and  vapor  given 
off  from  a  charge  of  boiling  liquor  passes  along  the  exhaust  pipe 
to  the  condenser  where  it  is  condensed.  Any  liquor  that  might 


AND    CONDENSERS    FOR   EVERY  SERVICE 


UNION       STEAM       PUMP       COMPANY 


1 


pass  over  with  the  vapor,  due  to  priming,  falls  in  the  liquor  trap 
from  which  it  is  returned  to  the  pan. 

In  order  to  maintain  a  vacuum  in  the  pan,  it  is  necessary 
to  remove  the  air  which  enters  the  condenser  from  the  liquid, 
from  the  cooling  water,  and  through  leaks.  For  this  purpose  a 
vacuum  pump  is  provided,  which  is  connected  to  the  condenser. 

Vacuum  pans  may  be  arranged  to  operate  on  either  the  dry 
or  wet  system.  When  the  dry  system  is  employed,  the  pan  is 
fitted  with  a  barometric  condenser,  and  the  vacuum  pump 
handles  only  the  noncondensable  vapors.  For  this  purpose  a 
dry  vacuum  pump  of  the  fly  wheel  type,  as  shown  in  figure  91, 
is  generally  used. 

There  are  installations,  however,  operating  on  the  dry 
system,  which  employ  a  wet  vacuum  pump,  either  of  the  fly 
wheel  type,  as  shown  in  figure  176  or  of  the  direct  acting  type, 
as  shown  in  figure  137a.  In  cases  of  this  kind  the  vacuum  pump 
handles  only  the  noncondensable  vapors,  and  it  is  provided  with 
a  small  quantity  of  charging  water  for  sealing  the  valves.  Figure 
138  illustrates  a  vacuum  pump  with  a  barometric  condenser 
operating  on  the  dry  system  with  a  direct  acting  vacuum  pump. 

The  vacuum  in  the  pans  operating  on  the  dry  system  varies 
up  to  28 ",  this  factor  depending  upon  the  nature  of  the  liquid 
to  be  evaporated. 

Vacuum  pans  operating  on  the  wet  system  are  fitted  with 
low  level  jet  condensers,  and  the  vacuum  pump  has  to  handle 
both  the  condensing  water  and  the  noncondensable  vapors. 
For  this  service  the  vacuum  pump  is  of  the  wet  type,  as  shown 
in  figure  137a,  or  of  the  fly  wheel  type  as  shown  in  figures  176 — 
178.  Vacuum  pans  operating  on  the  wet  system  generally  carry 
vacuum  of  25"  to  26  ". 

The  displacement  of  the  vacuum  pump  for  use  with  a 
vacuum  pan  on  the  wet  or  dry  system  is  based  on  the  amount 
of  liquor  to  be  evaporated. 

The  following  figures  give  the  approximate  displacement 
of  the  vacuum  pump  based  on  the  liquor  to  be  evaporated. 

Wet  System 

25  *  of  vacuum    60—1 
26 "of  vacuum   70-1 


322 


1- 

B  A 

TTT 

F, 

C  REEK, 

M 

1CH 

IGAN, 

U. 

S. 

A. 

3 

Dry  Sysiem 

25  "  of  vacuum   31-1 

26  "  of  vacuum   37^-1 
27//of  vacuum   47-1 
28  "  of  vacuum   55—1 

The  amount  of  steam  required  to  evaporate  various  quanti- 
ties of  liquor,  and  the  number  of  gallons  of  cooling  water  for 
condensing  purposes  is  given  in  the  table  on  page  329. 


iL 


Fig.  138 

Cut  Showing  a  Vacuum  Pan  with  Equipment  of  Pumps  Operating  on 
the  Dry  Sys.em  with  a  Wet  Vacuum  Pump. 

Multiple  Effect  Evaporator 

Instead  of  evaporating  a  liquid  in  a  single  effect  vacuum 
pan, quite  often  the  process  is  distributed  through  several  effects, 
two,  three  or  four,  with  the  result  that  there  is  a  large  saving 
made  in  the  consumption  of  steam  required  to  evaporate  the 
liquor  and  consequently  in  the  fuel  necessary  for  the  production 
of  steam.  This  saving  is  more  marked  when  the  liquid  to  be 
concentrated  is  of  a  low  density. 


AND    CONDENSERS:,FOR   EVERY  SERVICE 


323 


324 


The  principle  upon  which  the  multiple  effect  pan  works  is 
the  well  known  physical  law  that  the  latent  heat  of  vapor  is 
given  off  in  condensing  to  a  liquid,  while  the  sensible  heat 
is  retained.  Hence  the  employment  of  either  live  steam  from 
the  boiler  or  exhaust  steam  from  the  engine  for  heating  the 
first  pan  or  effect,  and  that  resulting  from  the  evaporation  of 
the  liquid  itself  that  is  introduced  into  the  apparatus  for  con- 
centration for  heating  the  succeeding  pans  or  effects,  each  effect 
after  the  first  thus  forming  a  condenser  to  the  previous  one, 
and  its  condensing  power  regulates  the  evaporating  capacity 
of  the  other. 

The  principle  of  operation  of  a  multiple  effect  evaporator 
is  clearly  shown  in  figure  139,  which  illustrates  a  diagrammat- 
ical view  of  a  triple  effect  evapprator.  These  pans,  which  are 
cylindrical,  are  provided  with  two  tube  plates,  one  of  which  is  set 
in  the  lower  end  of  the  pan,  and  the  other  at  about  the  center 
of  the  pan.  The  space  between  the  tube  plates  forms  a  calandria, 
or  heating  chamber  L  into  which  steam  is  introduced  for  heating 
purposes.  G  are  tubes  secured  in  the  tube  heads,  which  form 
communication  between  the  upper  or  lower  portions  of  the  pan. 
From  the  diagram  it  can  be  seen  that  the  liquid  to  be  evaporated 
circulates  above  and  below  the  tube  plates,  and  through  the 
tubes,  while  the  steam  or  heating  vapor  circulates  between  the 
tube  plates,  and  around  the  exterior  of  the  tubes.  The  vacuum 
pans  No.  1,  No.  2  and  No.  3  are  partially  filled  with  liquor, 
thus  leaving  in  the  upper  part  of  each  a  space  for  receiving  the 
vapor  produced  by  the  evaporation  of  the  liquor.  These  spaces 
are  connected  by  pipes  A  in  the  case  of  the  pans  No.  1  and  No.  2 
with  the  heating  space  L  of  the  pan  next  in  order,  and  in  that 
of  the  last  pan  No.  3  with  the  condenser  P,  in  which  the  vapors 
are  condensed,  and  the  air  is  drawn  off  by  the  air  pump.  The 
connecting  pipes  A  between  the  pans  are  fitted  with  traps  H 
to  catch  any  of  the  liquor  which  might  pass  over  with  the  vapor 
through  priming,  pipes  S  returning  any  liquor  carried  over 
from  the  traps  to  the  pans.  The  liquor  spaces  of  the  calandria 
of  the  three  pans  are  connected  together  by  pipes  K.  C  is  the 
steam  supply  pipe  to  the  heating  space  of  the  first  pan  No.  1, 
and  B  is  the  pipe  for  charging  the  first  pan  with  liquor  to  be 
concentrated.  T  is  a  pipe  which  is  connected  by  a  suitable 
branch  to  a  well  in.  the  bottom  of  each  of  the  three  effects,  and  by 


KKiaaH^^en|jnai3:^nac^auaaai2QiMci3ijai^anE^^aL^EC^n^^^^^^^S^^^^M^Si^^1 

AN D    <g Q N_D.ENjS_E RS^.FOR    E VE R V_ S E RVI GET 


325 


means  of  which  any  one  of  the  set  can  be  emptied,  if  desired. 
M  is  a  pipe  for  removing  the  concentrated  syrup  from  the  last 
effect  No.  3.  J  is  the  by-pass  pipe  connecting  the  heating  space 
of  the  calandria  L  of  the  No.  1,  No.  2  and  No.  Span.  E.  D. 
and  M.  are  pipes  for  removing  the  condensed  steam,  or  vapor 
from  the  calendria  L.  N  is  a  by-pass  pipe  is  the  No.  3  pan 
connecting  the  tipper  part  of  the  calendria  L  to  the  upper 
part  of  the  pan,  for  removing  the  n  on  condensable  vapors. 

The  operation  of  the  multiple  effect  evaporator  shown  is 
as  follows:  The  exhaust  or  waste  steam  is  usually  employed 
for  heating  the  first  effect  No.  1.  This  steam  is  delivered  into 
the  heating  space  of  the  calandria  L  of  part  No.  1  where  it 
circulates  around  the  tubes  G,  and  the  condensation  is  drawn 
out  through  the  pipe  D,and  is  delivered  to  a  tank  from  which  it  is 
returned  to  the  boilers.  The  steam  or  vapor  given  off  by  the  boil- 
ing liquor  in  pan  No.  1  passes  through  pipe  A  to  the  heating  space 
of  the  calandria  L  of  the  second  pan  No.  2,  where  it  circulates 
around  the  tubes  G,  and  then  passes  through  the  pipe  J  to  the 
heating  space  L  of  the  third  pan  No.  3,  and  together  with  the 
vapor  given  off  by  the  boiling  liquor  in  the  second  pan  No.  2, 
which  also  passes  to  the  heating  space  through  the  pipe  A, 
circulates  around  the  tubes  G. 

The  noncondensable  vapors  are  drawn  off  by  the  air  pump 
from  the  heating  space  L  of  the  No.  3  pan  through  the  pipe  N. 
The  steam  or  vapor  given  off  from  the  boiling  liquor  in  the 
third  or  last  pan  No.  3  passes  through  the  pipe  A  to  the  condenser 
P  where  it  is  condensed.  The  condensed  steam  or  vapor  and 
the  condensing  water  fall  through  the  tail  pipe  U,  while  the  non- 
condensable  vapors  are  withdrawn  by  the  air  pump  through 
the  pipe  Q.  The  juice,  or  liquor  passes  through  the  apparatus 
from  one  pan  to  another  through  the  pipes  K,  on  account  of  the 
difference  of  vacuum,  and  the  concentrated  liquor  is  withdrawn 
from  the  last  effect  through  the  pipe  F.  by  a  thick  liquor  pump. 

This  apparatus  is  usually  so  arranged  that  it  can  be  also 
worked  as  a  double  effect,  or  either  pan  singly  if  desired. 

When  employed  as  a  triple  effect  evaporator,  the  first  pan 
No.  1  generally  has  a  vacuum  of  three  or  four  inches,  and  a 
temperature  of  200°  .,  the  second  pan  No.  2  generally  has 
a  vacuum  of  about  14",  and  a  temperature  of  about  180° 


I ......  .?.VMf!??f ] .  .^.^H  ff.1.^ ^ S2Guut^J^££^S^^^&§^^JB i 

326 


ana  tne  third  pan  No.  3  generally  has  a  vacuum  of  about  26",  and 
a  temperature  of  about  125°  . 

It  will  be  seen  from  this  explanation  that  the  effect  is  largely 
self  heating,  that  is,  the  first  pan  only  is  heated  by  extraneous 
means,  the  latent  heat  of  the  vapor  from  the  boiling  liquor  in 
the  first  pan  being  utilized  to  heat  the  liquor  in  the  next,  or 
second.  The  latent  heat  of  the  steam  from  the  liquor  in  the 
second  to  heat  that  in  the  third.  Not  taking  into  considera- 
tion the  loss  of  heat  experienced  by  radiation,  a  double  effect 
is  twice,  and  the  triplicate  effect  three  times  as  economical  of 
steam  as  the  single  effect. 

Multiple  effect  evaporators  are  operated  on  both  the  wet 
and  dry  system,  the  same  as  vacuum  pans,  as  described  on 
page  322,  and  both  the  wet  and  dry  vacuum  pumps  are  em- 
ployed, the  type  depending  upon  the  installation. 

While  the  displacement  of  the  vacuum  pump  on  a  multiple 
effect  evaporator  depends  on  the  number  of  effects,  the  figures 
given  on  page  322  may  be  used  for  calculating  the  displacement 
of  the  vacuum  pump  for  multiple  effect  evaporators  based  on  the 
total  amount  of  liquor  to  be  evaporated. 

The  amount  of  steam  to  use  with  multiple  effect  evapora- 
tors, as  well  as  the  quantity  of  condensing  water  is  given  in  the 
table  on  page  329. 


327 


1 

w 

.S 

j 


328 


d 

ATTLE 

C  R 

EE 

K. 

M 

ICH 

[CAN, 

U. 

S. 

A. 

II 

Economy  Rating  of  Evaporators* 

Steam  Consumption  of  Evaporators  and  Cooling  Water 

Requirements  of  Condensers 


JSteam  Consumed 

2"c5 
oO 

Pounds  per  Hour 

fCooling  Water  to  Condenser—  U.S.  Gallons 

o.  . 

£ 

per  Minute 

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WPS 

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*cL 

Single  Effect 

Double  Effect 

Triple  Effect 

Quad.  Effect 

Isl 

£c? 

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W 
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3 

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Temp,  of  Injec- 
tion— °F. 

Temp,  of  Injec- 
tion —  °F. 

Tern,  of  Injec- 
tion— OF. 

Tem.of  Injec- 
tion —  °F. 

*  2« 
ft  £  a 

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1 

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H 

3*e 
ow 

60 

70 

80 

60 

70 

80 

60 

70 

80 

60 

70 

80 

100 

925 

465 

310 

230 

42 

52 

70 

21 

26 

35 

14 

17 

23 

11 

13 

18 

150 

1390 

695 

465 

345 

63 

78 

105 

32 

39 

53 

21 

26 

35 

16 

20 

26 

200 

1850 

925 

620 

465 

84 

104 

140 

42 

52 

70 

28 

35 

47 

21 

26 

35 

300 

2775 

1390 

925 

695 

126 

156 

210 

63 

78 

105 

42 

52 

70 

32 

39 

53 

400 

3700 

1850 

1230 

925 

168 

208 

280 

-84 

104 

140 

56 

69 

95 

42 

52 

70 

500 

4625 

2315 

1540 

1160 

210 

260 

350 

105 

130 

175 

70 

87 

115 

53 

65 

88 

750 

6940 

3475 

2315 

1730 

290 

360 

480 

160 

195 

205 

105 

130 

175 

79 

98 

130 

1000 

9250 

4630 

3080 

2310 

390 

480 

640 

210 

260 

350 

140 

175 

235 

105 

130 

175 

1250 

11560 

5780 

3860 

2890 

490 

600 

800 

245 

300 

400 

175 

215 

290 

130 

165 

220 

1500 

13880 

6940 

4630 

3470 

585 

720 

960 

295 

360 

480 

210 

260 

3f)0 

160 

195 

265 

2000 

18500 

9250 

6170 

4630 

780 

960 

1280 

390 

480 

640 

260 

32U 

425 

210 

260 

350 

2500 

23130 

11570 

7710 

5790 

975 

1200 

1600 

490 

600 

800 

325 

400 

535 

245 

300 

400 

3000 

27750 

13880 

9250 

6940 

1170 

1440 

1920 

585 

720 

960 

390 

480 

640 

295 

360 

480 

4000 

37000 

18500 

12340 

9250 

1560 

1920 

2560 

780 

960 

1280 

520 

64*0 

855 

390 

480 

640 

5000 

46250 

23130 

15400 

11560 

1950 

2400 

3200 

975 

1200 

1600 

650 

800 

1065 

490 

600 

800 

6000 

55500 

27750 

18500 

13880 

2340 

2880 

3840 

1170 

1440 

1920 

780 

960 

1280 

585 

720 

9GO 

7000 

64750 

32380 

21580 

16190 

2730 

3360 

4480 

1365 

1680 

2240 

910 

1120 

1495 

685 

840 

1120 

8000 

74000 

37000 

24670 

18500 

3120 

3840 

5120 

1560 

1920 

2560 

1040 

1280 

1705 

780 

960 

1280 

9000 

83250 

41630 

27750 

20810 

3510 

4320 

5760 

1305 

2160 

2880 

1170 

1440 

1920 

880 

1080 

1440 

10000 

92500 

46250 

30840 

23130 

3900 

4800 

6400 

1950 

2400 

3200 

1300 

1600 

2135 

975 

1200 

1600 

12000 

111000 

55500 

37000 

27750 

4680 

5760 

7680 

2340 

2880 

3840 

1560 

1920 

2560 

1170 

1440 

1920 

Swenson  Evaporator  Co . 


*Figures  in  thw  table  do  not  represent  the  best  performances  of  evaporators  and  con- 
densers; but  are  compiled  with  reasonable  allowance  for  the  fluctuations  and  variations 
of  average  practice.  Steam  and  cooling  water  requirements  will  often  be  found  less,  and 
sometimes  somewhat  more,  than  indicated  Steam  consumption,  for  instance,  varies  with 
different  efficiencies  of  heat  insulating  covering  employed;  while  cooling  water  requirements 
are  affected  by  air  content  of  the  injection  water,  and  other  factors.  Any  data  obtained 
from  this  table  will  be  found  to  agree  closely .  with  data  generally  obtained  from  actual 
ooeration. 

**In  the  case  of  a  multiple  effect,  figures  given  are  for  combined  vaporation  from 
all  effects. 

JAmount  of  heating  steam  supplied  to  first  effect,  at  pressure  of  3  to  5  pounds,  when 
liquor  is  fed  to  evaporator  at  approximately  120  degrees  F.  Different  steam  pressure,  or 
reasonably  different  temperature  of  feed  liquor  will  affect  figures  within  a  few  percent  only. 

tBased  on  26-inch  vacuum  (referred  to  30-inch  barometer)  in  last  effect.  Figures 
above  heavy  black  line  are  for  parallel  current  jet  condensers,  below  heavy  black  line  for 
counter  current  condensers.  The  type  of  condenser  usually  employed  is  as  indicated  by  this 
statement. 


F  OR    EVE  FLY  S  E RV I C E 


P     UNION 

STEAM 

P  UM  P 

COM  P  ANY 

4 

^Steam  Table  for  Evaporator  Work 


Vacuum  — 
Referred    to 
30"  B  Mercury 
at  58.4  Pahr. 

Temperature 

Specific 
Volume 

Heat  of  the 
Liquid 

Heat  of 
Vaporization 

Inches 

Mill- 
meters 

°Fahr. 

°Cent. 

Cu.Ft. 
per  Ib. 

Cu.M. 
per  Kilo 

B.T.U. 
per  Ih. 

Calories 
per  Kilo 

B.T.U 
pelb.. 

Calories 
pi  Kilo 

29.0 
28.  5 
28.0 

736.6 
723.9 
711.2 

79.07 
91.70 
101.15 

26.11 
33.17 
38.42 

657 
446.2 
339.6 

41.02 
27.86 
21.20 

47.11 
59.70 
69.12 

26.17 
33.17 
38.40 

1047.2 
1040.3 
1035.0 

581.8 
577.9 
575.0 

27.5 
27.0 
26.5 

698.5 
685.8 
673.1 

108.70 
115.06 
120.55 

42.61 
46.14 
49  .  20 

275.2 
231.9 
200.2 

17.18 
14.48 
12.50 

76.64 
82.98 
88  .  46 

42.58 
46.10 
49.14 

1030.8 
1027.2 
1024.1 

572.7 
570.7 
568.9 

26.0 
25.5 
25.0 

660.4 
647.7 
635.0 

125.38 
129.75 
133  .  77 

51.88 
51.3! 
56.  5  1 

176.7 
158.1 
113.0 

11.03 

9.870 
8.927 

93  .  28 
97.64 
101.65 

51.82 
54.24 
56.47 

1021.4 
1018.9 
1016.7 

567.4 
566  .  1 
564.8 

24.0 
23.0 
22.0 

~21.0 
20.0 
19.0 

609.6 
584.2 
558.8 

140.64 
146.78 
152.16 

60  .  38 
63.77 
66.76 

120.9 
104.5 
92.3 

7.548 
6.524 
5.762 

108.51 
114.64 
120.02 

60.28 
63.69 
66.69 

69  .  37 
71.82 
74.04 

1012.8 
1009.3 
1006.2 

562.7 
560.7 
559.0 

533.4 
508.0 
482.6 

157.00 
161.42 
165.42 

169.14 
172.63 
175.93 

69  .  44 
71.90 
74.12 

82.6 
74.8 
68.5 

5.157 
4.670 
4.276 

124.86 
129.28 
133.28 

137.00 
1  10  .  50 
143.80 

1003.4 
1000  .  8 
998.5 

557  .  4 
556.0 
554.7 

553  .  6 
552.5 
551.3 

18.0 
17.0 
16.0 

457.2 
431.8 
406.4 

76.19 
78.13 
79.94 

63.1 
58.6 
54.6 

3.939 
3.658 
3.409 

76.11 
78.06 
79.89 

996.4 
994.3 
992.3 

15.0 
14.0 
13.0 

12.0 
11.0 
10.0 

381.0 
355.6 
330.2 

304.8 
279.4 
254.0 

179.03 
181.92 
184.68 

81.69 
83.29 
84.82 

51.2 
49.0 
45.55 

43.2 
41.05 
39.1 

3.196 
3.059 

2.844 

2.  699 
2  .  563 
2.441 

146.91 
149  .  SO 
152.57 

81.62 
83.22 
84.76 

990.5 

98.8  .  8 
987.1 

550.3 
549.3 
548.4 

187.31 
189  .  83 
192.23 

86.28 
87.68 
89.02 

155.21 
157.73 
160.14 

86.23 
87.63 
88.97 

985  .  5 
984.0 
982.2 

547.5 
546.7 
545.6 

9.0 
8.0 
7.0 

6.0 
5.0 
4.0 

228.6 
203.2 
177.8 

152.4 
127.0 
101.6 

191.52 
196.73 
198.87 

90.29 
91.52 
92.70 

37.4 
35.8 
34.3 

2.335 
2.235 
2.141 

162.44 
164.68 
160.81 

168.88 
170  .  89 
172.81 

90  .  24 
91.49 
92.67 

93  .  82 
94.93 
96.06 

981.2 
979  .  8 
978.6 

977.2 
976  .  1 
974.8 

545  .  1 
544.3 
543.7 

200  .  94 
202.92 
204  .  85 

93.86 
94.96 
96.03 

83  .  0 
31.8 
30.6 

2.060 
1.985 
1.910 

542  .  9 
542.3 
541.6 

3.0 
2.0 
1.0 
0.0 

76.2 
50.8 
25.4 
0.0 

206.71 
208  .  52 
210.28 
212.00 

97.06 
98.07 
99.04 
100.00 

29  .  55 
28.6 
27.7 
26.8 

1.845 
1.785 
1.729 
1.673 

174.68 
176  50 
178.27 
180.00 

97.04 
98.06 
99.04 
100.00 

973.7 
972.6 
971.4 
970.4 

540.9 
540.3 
539.7 
539.1 

Pressure 

215.3 

218.5 
221.5 

25.23 
23  .  80 
22.53 

537  .  9 
536.8 
535  7 

Lbs.  per 
Sq.  In. 
Gauge 

1 
2 
3 

Atmos- 
spheres 

.068 
.136 
.204 

101.8 
103.6 
105.3 

1.575 
1.486 
1.407 

183.4 
186.6 
189.6 

101.9 
103.7 
105.3 

968.2 
966.2 
964.3 

4 
5 
6 

.272 
.340 
.408 

224.4 
227.2 
229.8. 

106.9 
108.4 
109.9 

21.40 
20.38 
19.45 

1  .  336 
1.272 
1.214 

192.5 
195.3 
198.0 

106.9 
108.5 
110.0 

962.4 
960.6 
958.8 

531.7 
533  .  7 
532  .  7 

7 
8 
9 

.476 
.544 
.612 

232.4 
234  8 
237.1 

111.3 
112.7 
113.9 

18.61 
17.85 
17.14. 

1.162 
1.114 
1.070 

1.029 
.8660 

.7485 

200.6 
203.1 
205.4 

111.4 
112.8 
114.1 

115.4 
121.2 
126.3 

135.0 
142.2 

148.4 

957.2 
955.2 
954.0 

952.5 
945.5 
939.3 

531.8 
530  .  7 
530  .  0 

529.2 
525.3 

521.8 

515.8 
510.8 
506.2 

10 
15 
20 

1.680 
2.021 
2.361 

239.4 
249.7 
258.8 

115.2 
120.9 
126.0 

16.49 
13.88 
11.99 

9.45 
7.82 
6.68 

207.7 
218.2 
227  .  4 

243.0 
255.9 
267.2 

30 
40 
50 

3.041 
3.722 
4.402 

274.1 

286.7 
297.7 

134.5 
141.5 
147.6 

.5900 

.4882 
.4169 

928.5 
919.4 
911.2 

60 
70 
80 

5.082 
5.763 
6.443 

307.3 
316.0 
323.9 

152.9 
157.8 
162.2 

5.83 
5.18 
4.67 

.3640 
.3234 
.2915 

277  .  1 
286.1 
294.3 

153.9 
158.9 
163.5 

903.9 
897.2 
891.0 

502.2 
498.4 
495.0 

90 

100 

7.124 

7  804 

331.2 
337.9 

166.2 
169.9 

4.24 
3.89 

.2647 
.2429 

301.8 
308  .  8 

167.7 
171.6 

885.3 
880.0 

491.8 

488.9 

*From  tables  given  by  Marks  &  Davis. 

B.  T.  U.  per  pound=.5555  Calories  per  kilo.          1  Cal.  per  kilo=l  8  B.  T.  U.  per  pound 
Cu.  Ft.  per  pound=.06243  Cu.  Meters  per  kilo.        1  Cu  Meter  per  Kilo=16.018<f  Cu.  Ft.  pe 


1 
ICu. 


per  pound- 


330 


RATTLE       C  REEK.     M  1C  H  I  G  AN.      U.  S.  A.~ 


Boiling  Points  of  Liquids  (Degrees  Cent.)  at 

Atmospheric  Pressure,  and  under  various 

Degrees  of  Vacuum 


LIQUID 

Atmos- 
pheric 
Pressure 

20.7  inches 
of  Vacuum 

24  inches 
of  Vacuum 

28  inches 
of  Vacuum 

29i  inches 
of  Vacuum 

Water  

100 

70 

60.3 

38.4 

14   87 

Alcohol 

78  2 

51 

42 

24 

-3  1 

Ether 

35 

5 

-5 

-25 

-55 

Acetic  Acid 

119  7 

84  58 

73   17 

49  84 

15 

Benzine 

80  36 

46  6 

35  36 

12  86 

-21 

Oil  of  Turpentine  
Butyric  Acid  
Glycerin  

159 
161.7 
290 

119.28 
124.86 
252  5 

106 
111.6 

240 

79.8 
87 
215 

29.54 
51.2 
177  5 

Mercury  

357  25 

297  25 

277  25 

237  25 

177  25 

Naphol  

290 

230 

210 

170 

110 

Carbolic  Acid  
Cresol 

178 
190 

142 
154 

130 
145 

104 
118 

70 

82 

Useful  Data 

1  standard  atmosphere  (by  definition)  =  760  mm.  of  mercury 
at  0°  Cent.  =  29.921 "  mercury  at  32°  F.  =30.000 "  mercury  at 
58.4°  F.  =33.90  ft.  water  at  32°  F.  =  14.696  pounds  per  sq.  in. 


Pressure  Conversion  Factors  at  32°  F. 


Inches 
Mercury 

Feet 
Water 

Pounds 
per  sq.  in. 

Atmospheres 

Inches  Mercury 

1 

1.133 

.491 

.0334 

Feet  Water 

.8827 

1 

.434 

.0295 

Lbs.  per  sq.  in. 

2.037 

2.308 

1 

.0680 

Approximate  temperature  correction  factor  for  height  of 
a  mercury  column  =.0001  per  degree  F. 

Example  ~  Barometer  reads  30.00  "  at  80°  F.  To  correct 
reading  to  58.4°  F.  Correction  =  .0001 X  30  X  (80—58.4)  = 
0  648".  Reading  at  58.4°  F.  =  30.00*  +  . 065 "  = 30.065''. 


AND   CONDE N  S  E R  S    F  O  R   E  VE R Y.  S  E RV I CB 


Reduction  of  Barometer  to  Sea  Level 

Mean  Temperature  of  the  Air  Column  58°P. 
Calculated  from  values  given  by  Smithsonian 
Meteorological  Tables 


Elevation  in  feet 

0 

500 

1000 

2000 

3000 

4000 

5000 

6000 

7000 

8000 

9000 

Barometer  read- 
ing in  inches  mer- 
cury at  58.4°  F. 
equivalent  to  30* 
reading  at  sea 
level. 

30. 

29.45 

28.95 

27.9 

26.95 

26. 

25.1 

24.2 

23.3 

22.5 

21.7 

Elevation  in  Feet  at  Various  Points  in  the  United  States  as  Given 
by  the  U.  S.  Geological  Survey 


Albuquerque,  N.  M 4943 

Atlanta,  Ga 1032 

Birmingham,  Ala 600 

Boise,  Ida 2695 

Buffalo,  N.  Y 583 

Butte,  Mont 5576 

Cheyenne,  Wyo 6062 

Chicago,  111 590 

Cincinnati,  Ohio 490 

Dallas,  Texas 425 

Denver,  Colo 5183 

Des  Moines,  la 803 

Detroit,  Mich 579 

Duluth,  Minn.. 609 

Helena,  Mont 4009 

Indianapolis,  Ind 708 

Kansas  City,  Mo 750 

Knoxville,  Tenn 890 


Leadville,  Colo 10185 

Lexington,  Ky 946 

Minneapolis,  Minn 812 

New  York,  N.  Y 54 

Ogden,  Utah 4296 

Oklahoma  City,  Okla 1197 

Omaha,  Neb 1034 

Phoenix,  Ariz 1082 

Pittsburgh,  Pa 743 

Pocatello,  Ida 4461 

Portland,  Ore 29 

Pueblo,  Colo 4660 

Reno,  Nev 4491 

Salt  Lake  City,  Utah 4248 

San  Francisco,  Calif .        15 

Santa  Fe,  N.  M 6947 

Searles  Lake,  Calif 1805 

Spokane,  Wash 1909 


B^J^^-lSJL^-5^^^ 


332 


B  A  T  T  LE      CREEK.     MICHIGAN 


Comparison  of  Various  Hydrometer  Scales 


Specific  ( 

Gravities 

o 

0 

0) 

6 

3 
J 

-°            PG 
.  •           i 

O 

0 

10 
1C 

|f 

Us  f 

Soo    pq 
N'^    1 

'§S 

ij 

PQ 

CO 

T^<£? 

ool 

Q; 

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E.S       1 

5      1^ 

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g 

-fg^-S    !£ 

2j| 

e 

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°e  r 

PQ      bi 

co-^' 

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*.g 

'tn 
a 
$ 

"H*"* 

•S-c     a 

£      d 

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Jrt            W            U 

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P 

£-H  C<) 

PQ  >>    co 

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PQ   JrJ 

.j     d 

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| 

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i 

fi& 

*f  H-*                 t/3 

§ 

bi 

bo 

!j 

CiO 

o 

3 

& 

&" 

& 

0 

1.000 

1.0000 

0.0 

0.0 

0.0 

0.0 

0.0 

0.0 

1 

1.007 

1.0070 

0.7 

1.4 

2.8 

1.2 

1.8 

0.4 

2 

1.014 

1.0140 

1.4 

2.8 

5.5 

2.3 

3.6 

1.4 

3 

1.021 

1.0215 

2.1 

4.2 

8.2 

3.5 

5.4 

2.1 

4 

1.028 

1.0285 

2.8 

5.6 

10.9 

4.6 

7.1 

2.7 

5 

1.036 

1.0380 

3.6 

7.2 

13.9 

5.9 

9.0 

3.5 

6 

1.043 

1.0435 

4.3 

8.6 

16.5 

7.0 

10.7 

4.1 

7 

1.051 

1.0510 

5.1 

10.2 

19.4 

8.3 

12.6 

4.8 

8 

1.058 

1.0585 

5.8 

11.6 

21.9 

9.3 

14.3 

5.5 

9 

1.066 

1.0665 

6.6 

13.2 

24.8 

10.4 

16.1 

6.2 

10 

1.074 

1.0745 

7.4 

14.8 

27.5 

11.7 

18.0 

6.9 

11 

1.082 

1.0825 

8.2 

16.4 

30.3 

12.9 

19.8 

7.6 

12 

1.090 

1.0905 

9.0 

18.0 

33.0 

14.1 

21.5 

8.3 

13 

1.098 

1.0990 

9.8 

19.6 

36.0 

15.2 

23.3 

8.9 

14 

1.107 

.1075 

10.7 

21.4 

39.0 

16.4 

25.2 

9.7 

15 

.115 

.1160 

11.5 

23.0 

41.3 

17.6 

27.0 

10.3 

16 

.124 

.1245 

12.4 

24.8 

44.2 

18.8 

28.9 

11.0 

17 

.133 

.1335 

13.3 

26.6 

46.5 

20.0 

30.7 

11.7 

18 

.142 

.1425 

14.2 

28.4 

49.7 

21.2 

32.6 

12.4 

19 

.151 

1.1515 

15.1 

30.2 

52.5 

22.3 

34.4 

13.1 

20 

.160 

1.1607 

16.0 

32.0 

55.2 

23.5 

36.2 

13.8 

21 

.169 

1.1705 

16.9 

33.8 

57.8 

24.6 

38.0 

14.5 

22 

.179 

1.1795 

17.9 

35.8 

60.7 

25.8 

40.0 

15.2 

23 

.188 

1.1895 

18.8 

37.6 

-    63.3 

26.9 

41.7 

15.8 

24 

.198 

1.1995 

19.8 

39.6 

66.1 

28.1 

43.6 

16.5 

25 

.208 

1.2095 

20.8 

41.6 

68.9 

29.3 

45.5 

17.2 

26 

.218 

1.2195 

21.8 

43.6 

71.6 

30.4 

47.3 

17.9 

27 

.229 

1.2300 

22.9 

45.8 

74.5 

31.7 

49.4 

18.6 

28 

.239 

1.2405 

23.9 

47.8 

77.2 

32.8 

51.2 

19.3 

29 

.250 

1.2515 

25.0 

50.0 

79.3 

34.0 

53.2 

20.0 

30 

.261 

1.2625 

26.1 

52.2 

82.8 

35.2 

55.1 

20.7 

31 

1.272 

1.2735 

27.2 

54.4 

85.5 

36.4 

57.0 

21.4 

32 

1.283 

1.2850 

28.3 

56.6 

88.3 

37.5 

58.9 

22.1 

33 

1.295 

1.2960 

29.5 

59.0 

91.1 

38.8 

60.9 

22.8 

34 

1.306 

1.3080 

30.6 

61.2 

93.7 

39.9 

62.7 

23.4 

35 

1.318 

1.3200 

31.8 

63.6 

96.5 

41.0 

64.7 

24.1 

36 

1.330 

1.3320 

33.0 

66.0 

99.2 

42.2 

66.7 

24.8 

37 

1.342 

U3445 

34.2 

68-4 

101.9 

43.3 

68.6 

25.5 

AND    CONDENSERS 

.B»tn.uvy»v»«tt»w,»g1,  „»»»„.»»»»»«»» 


FOR    EVERY  SERVICE 


333 


STEAM      PUMP 


Comparison  of  Various  Hydrometer  Scales 
'Continued) 


Specific   Gravities 

o 

.. 

_o 

0) 

i 

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u 

g^ 

0 

X 

g 

0 

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60 

Jj 

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a 

a 

38 

1.355 

1.3570 

35.5 

71.0 

104. 

7 

44 

.6 

70.7 

26 

.2 

39 

1.368 

1.3700 

36.8 

73.6 

107. 

G 

45.8 

72.7 

26 

9 

40 

.381 

]  .3830 

38  1 

76.2 

110. 

3 

46 

.9 

74.7 

27 

.6 

41 

.394 

1  .  3955 

39  4 

78.8 

113. 

5 

48 

.0 

76.7 

28 

.3 

42 

.408 

1.4100 

40.8 

81.6 

115. 

9 

49 

.3 

78.8 

28 

.9 

43 

.421 

.4240 

42.1 

84.2 

118. 

5 

50 

.4 

80.8 

29 

.G 

44 

.436 

.4380 

43.5 

87.0 

121.3 

51 

.5 

82.9 

30 

.3 

45 

.450 

.4525 

45.0 

90.0 

124. 

1 

52.8 

85.1 

31 

.0 

46 

.465 

.4675 

46.5 

93.0 

126. 

7 

53 

.9 

87.2 

31 

.7 

47 

1.479 

1.4827 

48.0 

96.0 

129.7 

55 

.1 

89.4 

32 

.4 

48 

1.495 

1.4980 

49.5 

99.0 

132. 

4 

56 

.3 

91.5 

33 

.1 

49 

1.510 

1.5135 

51.0 

102.0 

135. 

1 

57 

.4 

93.6 

33 

.8 

50 

.526 

1.5300 

52.6 

105.2 

137. 

9 

58 

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irTTTnr^Tnrir 

MAC 


334 


BATTLE      CREEK.     MICHIGAN.      U.S.A. 


Low  Vacuum  Pumps 

Low  vacuum  pumps  are  mostly  use  a  on  vacuum  heating 
systems.  This  type  of  pump  illustrated  in  figure  141a,  when 
connected  to  the  return  pipe  of  a  heating  system,  insures  a 
positive  circulation  of  steam  throughout  the  system,  and  does 
away  with  the  annoying  cracking  or  hammering  in  the  pipe 
line.  This  application  not  only  increases  the  efficiency  of  the 
system,  but  greatly  reduces  the  cost  of  operation,  and  returns 
the  condensed  steam  at  a  high  temperature  for  feeding  back 
to  the  boilers. 


Fig.  141a 
Low  Vacuum  Pump 


Fig.  141b 
Section  through  Vacuum  Cylinder  of  Low  Vacuum  Pump 


AND    CONDENSERS    FOR   EVERT  SERVICE 


335 


}         UN 

I  O 

N 

ST 

E  AM 

P 

UM 

P 

C 

O  M 

PANY 

J 

The  low  vacuum  pump,  however,  is  not  intended  to  deliver 
the  water  of  condensation  directly  to  the  boilers,  but  should  de- 
liver to  an  open  heater,  or  tank,  and  the  water  may  then  be  re- 
turned directly  to  the  boiler  by  means  of  a  regular  boiler  feed 
pump.  Where  there  is  no  heater,  the  vacuum  pump  may  dis- 
charge into  the  receiver  of  an  automatic  pump  and  receiver  as 
described  on  page  316.  The  condensate  is  then  automatically 
returned  to  the  boilers  without  further  attention.  Figure  142 
illustrates  a  diagram  of  a  vacuum  heating  system,  and  the 
vacuum  pump  and  boiler  feed  pump  connections  are  clearly  shown. 

Direct  and  Indirect  Radiation 

Hot  water  and  steam  heating  systems  are  classified  accord- 
ingly to  the  position  and  manner  in  which  the  radiators  are  used. 
The  system  which  is  probably  the  most  familiar  is  the  one  where- 
in the  radiators  are  placed  directly  within  the  space  to  be  heated. 
This  heating  is  accomplished  by  direct  radiation,  and  by  air  con- 
vection currents  through  the  radiator,  no  provision  being  made 
for  a  change  of  air  in  the  room.  This  is  known  as  a  direct  system, 
and  while  it  causes  movements  of  the  air  in  the  room,  it  produces 
no  real  ventilation. 

In  the  indirect  system,  the  heat  radiating  elementis  erected 
somewhat  distant  from  the  rooms  to  be  heated,  and  ducts 
carry  the  heated  air  from  the  radiator  to  the  rooms  heated 
either  by  natural  convection,  or  by  means  of  fan  or  blower 
pressure.  When  the  radiating  element  of  a  building  is  installed 
together  in  one  room  of  the  building,  and  each  room  has  its 
share  of  the  heat  forced  to  it  through  ducts  from  one  centralized 
fan  or  blower,  the  system  is  called  a  Plenum  System. 

Steam  Required  for  Heating  Systems 

In  calculating  the  steam  capacity  necessary  for  heating 
systems,  it  is  assumed  that  a  boiler  horse  power  is  equivalent 
to  the  evaporation  of  34^  pounds  of  water  from  and  at  212°. 

Since  the  evaporation  of  one  pound  of  water  from  and  at 
212°  .  requires  966  heat  units,  one  boiler  horse  power  is 
equivalent  to  33,317  heat  units. 

For  heating  purposes,  a  more  convenient  standard  of  power 
is  the  number  of  square  feet  of  radiating  surface.  Carpenter 


336 


AND   CONDENSERS.   FOR   EVERY'  SERyiCB 

337 


says  that  each  square  foot  of  direct  radiating  surface  gives  off 
220-280  heat  units  per  hour,  when  the  difference  of  temperature 
is  150°,  which  is  that  usually  existing  in  low  pressure  steam  heat- 
ing. About  two-thirds  as  much  is  given  off  by  one  square  foot 
of  hot  water  radiating  surface.  As  the  evaporation  of  one 
pound  of  water  requires  966  heat  units, there  is  evaporated  about 
one-third  of  a  pound  of  steam  for  each  square  foot  of  steam 
radiating  surface  per  hour,  hence,  one  boiler,  horse  pow.er  will 
be  sufficient  to  supply  somewhat  more  than  one  hundred  square 
feet  of  direct  radiating  surface;  that  is  we  can  consider  the 
boiler  horse  power  as  equal  to  100  square  feet  of  direct  steam 
radiation  with  sufficient  allowance  to  meet  ordinary  losses. 

In  the  indirect  system  of  heating  provided  with  blower, 
the  heater  will  condense  under  average  conditions  one  pound 
of  water  per  square  foot  of  surface  per  hour.  The  boiler  capacity 
required  is  usually  rated  on  the  supposition  that  it  will  need  to 
supply  1.5  pounds  of  steam  for  each  square  foot  of  surface  in  the 
radiator  per  hour,  in  which  case  23  square  feet  of  surface  would 
be  supplied  by  one  boiler  horse  power. 

Size  of  Pump  for  Heating  System 

To  determine  the  size  of  vacuum  pump  to  use  in  connection 
with  the  vacuum  heating  system,  it  is  customary  to  allow  one 
pound  of  condensation  for  each  square  foot  of  direct  radiation 
per  hour,  and  to  make  the  pump  displacement  four  to  five  times 
this  amount,  and  to  take  care  of  both  the  air  and  condensate  in 
the  system,  the  pump  should  handle  this  capacity,  when  oper- 
ating at  the  speed  recommended  on  page  292. 

The  size  of  steam  cylinder  to  operate  a  vacuum  pump  may  be 
calculated  by  assuming  the  vacuum  cylinder  works  against  15 
to  20  pounds  pressure  and  a  mechanical  efficiency  of  50  per- 
cent. 

Example 

Assume  we  have  a  vacuum  heating  system  containing 
30,000  square  feet  of  direct  radiation,  and  it  is  desired  to  find 
the  size  vacuum  pump  to  use.  Steam  pressure  available  100 
pounds. 


S^c^^^^^a^S^^^^^fM^xxiaD^a^KK^a^x^^^aac^i^Es^^TLxi^S^^naa^^g^^^^^ 
PUMPINGMAGHINER^VAIR^COMPRE^S  O  RS 


338 


BATTLE      CREEK.     MICHIGAN,      U.  S.  A. 


Solution 

30,000  X 1  =30,000  pounds  of  steam  per  hour. 

! =60  gallons  per  minute  of 'condensation. 

8.3X60 

Now  allow  the  pump  displacement  of  five  to  one,  the  pump 
must  have  a  displacement  of  5X60,  or  300  gallons  per  minute. 
Assuming  a  piston  speed  of  100  feet  per  minute  (see  page  292  for 
speeds  recommended  for  vacuum  pumps)  by  formula  51,  page 
293,  the  diameter  of  the  vacuum  piston  will  be 
"300 


=4.95^- 


100 


The  nearest  commercial  size  is  9"  diameter,  and  the  stand- 
ard stroke  is  12". 

Now  having  the  diameter  of  the  vacuum  cylinder,  we  may 
calculate  the  load  on  the  vacuum  piston  thusly, 

Area  of  9"  piston  =63  square  inches. 

63X20=1260  pounds  total  pressure. 

With  the  assumed  mechanical  efficiency  of  50 %,  the  load 
required  on  the  steam  piston  will  be 

1260    =2520  pounds 
.50 

"and  with  100  pounds  steam  pressure,  the  diameter  of  the  steam 
piston  will  be 

2520 
=25.2  Square  inches 

=  Area  of  5^  inch  piston. 

The  nearest  commercial  size  is  6  ",  so  the  size  of  the  vacuury 
pump  is  then  6X9X12. 

In  calculating  the  size  of  the  steam  cylinder  to  use  on  a 
vacuum  pump,  the  minimum  steam  pressure  to  be  carried 
should  be  used,  and  the  discharge  head,  including  frictional 
losses  should  be  taken  into  consideration. 

For  heating  systems  where  the  steam  pressure  runs  from  10 
to  20  pounds,  the  steam  cylinder  of  the  vacuum  pump  should 
be  calculated  amply  large  on  account  of  the  fact  that  the  con- 
densation is  excessive.  Electrically  driven  Pumps  are  gener- 
ally used  where  the  steam  pressure  is  low. 

The  following  table  gives  the  square  feet  of  external  radia- 
tion for  different  sizes  of  pipe. 


339 


Square  Feet  of  Radiating  Surface  of  Pipe 
per  Lineal  Foot 

On  all  lengths  over  one  foot,  fractions  less  than  tenths  are  added  to 
or  dropped. 


Size  of  Pipe 


Sp- 

H 

1 

1M 

ilA 

2 

2j^ 

3 

4 

5 

6 

7 

8 

1 

275 

.346 

434 

.494 

.622 

753 

.916 

1.175 

1.455 

1.739 

1.996 

2.257 

2 

5 

7 

9 

1 

1    ?, 

1.5 

-    1  8 

2  4 

2.9 

3.5 

4. 

4  5 

3 

8 

1. 

1    3 

1    5 

1    9 

?,  3 

2  7 

3   5 

4  4 

5.2 

6. 

6  8 

4 

1.1 

1.4 

1.7 

2 

2.5 

3. 

3.6 

4.7 

5.8 

7. 

8. 

9. 

5 

1.4 

1.7 

2.2 

2.4 

3.1 

3.8 

4.6 

5.8 

7.3 

7.7 

10. 

11.3 

6 

1.6 

2.1 

2.6 

2.9 

3.7 

4.5 

5.5 

7. 

8.7 

10.5 

12. 

13.5 

7 

1.9 

2.4 

3. 

3.4 

4.4 

5.3 

6.4 

8.2 

10.2 

12.1 

14. 

15.8 

8 

2.2 

2.8 

3.5 

3.9 

5. 

6. 

7.3 

9.4 

11.6 

13.9 

16. 

18.0 

9 

2.5 

3.1 

3.9 

4.4 

5.6 

6.8 

8.2 

10.6 

13.1 

15.7 

18. 

20.3 

10 

2  7 

3  5 

4  3 

4  9 

6  ? 

7  5 

9  1 

11  8 

14  6 

17.4 

20. 

9.?,  6 

11 

3. 

3.8 

4.8 

5.4 

6.8 

8.3 

10. 

12.9 

16. 

19.1 

22. 

24.9 

12 

3.3 

4.1 

5.2 

5.9 

7.5 

9. 

11. 

14.1 

17.4 

20.9 

24. 

27.1 

13 

3.6 

4.5 

5.6 

6.4 

8.1 

9.8 

11.9 

15.3 

18.9 

22.6 

26. 

29.4 

14 

3.8 

4.8 

6.1 

6.9 

8.7 

10.5 

12.8 

16.5 

20.3 

24.3 

28. 

31.6 

15 

4.1 

5.2 

6.5 

7.4 

9.3 

11.3 

13.7 

17.6 

21.8 

26.1 

30. 

33.9 

16 

4.4 

5.5 

6.9 

7.9 

10. 

12.0 

14.6 

18.8 

23.2 

27.8 

32. 

36.1 

17 

4.7 

5.9 

7.4 

8.4 

10.  C 

12.8 

15.5 

20. 

24.7 

29.5 

34. 

38.4 

18 

5. 

6.2 

7.8 

8.9 

11.2 

13.5 

16.5 

21.2 

26.2 

31.3 

36. 

40.6 

19 

5  ? 

6.6 

8  3 

9  4 

11    8 

14  3 

17  4 

22  3 

27  6 

33.1 

38. 

42  9 

20 

5.5 

6.9 

8.7 

9.9 

12.5 

15. 

18.3 

23.5 

29.1 

34.8 

40. 

45.2 

21 

5.8 

7.3 

9.1 

10.4 

13. 

15.8 

19.2 

24.7 

30.5 

36.5 

42. 

47.4 

22 

6. 

7.6 

9.6 

10.9 

13.7 

16.5 

20.2 

25.9 

32. 

38.3 

44. 

49.7 

23 

6.3 

8. 

10. 

11.3 

14.3 

17.3 

21.1 

27. 

33.5 

40. 

46. 

52. 

24 

6.6 

8.3 

10.4 

11.9 

14.9 

18. 

22. 

28.2 

34.9 

41.7 

48. 

54.2 

25 

6.9 

8.6 

10.9 

12.3 

15.6 

18.8 

22  9 

29.3 

36.3 

43.5 

50. 

56.4 

26 

7.1 

9. 

11.3 

12.8 

16.2 

19.5 

23.8 

30.5 

37.8 

45.2 

52. 

58.6 

27 

7.4 

9.4 

11.7 

13.3 

16.8 

20.3 

24.7 

31.7 

39.3 

47. 

54. 

61. 

28 

7.7 

9.7 

12.2 

13.8 

17.4 

21. 

25.6 

32.9 

40.7 

48.7 

56. 

63.2 

29 

8. 

10. 

12.6 

14.3 

18. 

21.8 

26.6 

34.1 

42.2 

50.4 

58. 

65.5 

30 

8.3 

10.4 

13. 

14.8 

18.7 

22.5 

27.5 

35.3 

43.6 

52.1 

60. 

67.7 

31 

8.5 

10.7 

13.5 

15.3 

19.3 

23.3 

28.4 

36.4 

45.1 

53.9 

62. 

70. 

32 

8.8 

11.1 

13.9 

15.8 

19.9 

24.1 

29.3 

37.6 

46.5 

55.6 

64. 

72.2 

33 

9.1 

11.4 

14. 

16.3 

20.5 

24.8 

30.2 

38.8 

48. 

57.4 

66. 

74.4 

34 

9.4 

11.7 

14. 

16.8 

21.2 

25.6 

31.1 

40. 

49.5 

59.1 

68. 

76.7 

35 

9.6 

12.1 

15. 

17.3 

21.8 

26.3 

32. 

41.1 

50.9 

60.8 

70. 

79. 

36 

9.9 

12.5 

15. 

17.8 

22.4 

27. 

33. 

42.3 

52.4 

62.6 

72. 

81.3 

37 

10.2 

12.8 

16. 

18.3 

23. 

27.8 

33.9 

43.5 

53.8 

64.3 

74. 

83.5 

38 

10.5 

13.2 

16. 

18.8 

23.7 

28.5 

34.8 

44.6 

55.2 

66. 

76. 

85.8 

39 

10.7 

13.5 

16. 

19.3 

24.3 

29.3 

35.7 

45.8 

56.7 

67.8 

78. 

88. 

40 

11. 

13.8 

17. 

19.8 

24.9 

30.1 

36.6 

47. 

58.2 

69.5 

80. 

90.2 

41 

11.3 

14.2 

17. 

20.3 

25.5 

30.8 

37.6 

48.2 

59.6 

71.3 

82. 

92.5 

42 

11.5 

14.5 

18. 

20.8 

26.1 

31.6 

38. 

49.4 

61.1 

73. 

81. 

94.8 

43 

11.8 

14.9 

18. 

21.3 

26.8 

32.3 

39. 

50.6 

62.5 

74.8 

86. 

97. 

44 

12.1 

15.2 

19. 

21.8 

27.4 

33.1 

40. 

51   7 

64. 

76.5 

88. 

99.3 

45 

12.4 

15.6 

19. 

22.2 

28. 

33.8 

41. 

52.9 

65.5 

78.2 

90. 

101.6 

46 

12.7 

15.9 

20. 

22.7 

28.6 

34.6 

42. 

54. 

67. 

80. 

92. 

103.8 

47 

12.9 

16.3 

20.4 

23.2 

29  2 

35.3 

43. 

55.2 

68.4 

81.7 

94. 

106. 

48 

13.2 

16.6 

20.8 

23.7 

29.9 

36.1 

43.9 

56.4 

69.8 

83.5 

96. 

108.4 

49 

13.. 

17. 

21.3 

24.2 

30.5 

36.8 

44.8 

57.6 

71.2 

85.1 

98. 

110.5 

53 

13.8 

17.3 

21.7 

24.7 

31.1 

37.6 

45.8 

58.7 

72.7 

87. 

100. 

112.8 

340 


|        B  A  T  T  L  E 

C 

RE 

EK. 

M 

1C 

H 

1C 

AN. 

U. 

s. 

A 

Hydraulic  Pressure  Pumps 

Hydratilic  pressure  pumps  are  generally  used  with  hydraulic 
presses,  and  accumulators  in  connection  with  hydraulic  presses. 

For  this  work  a  pump  of  small  capacity  is  generally  required 
and  the  pressure  against  which  it  operates  varies  from  500 
up  to  5000  Ibs.  per  square  inch.  For  pressures  up  to  2000  Ibs. 
per  square  inch  the  hydratilic  pressure  pump  with  cast  iron 
cylinder  is  used,  and  for  pressures  above  this  a  hydraulic  pump 
with  either  a  cast  or  forged  steel  cylinder  is  used. 

The  purpose  of  the  accumulator  is  to  furnish  a  momentary 
demand  for  water,  which  the  hydraulic  pressure  pumps  can 
replenish,  when  the  hydraulic  press  is  not  in  operation.  The 
accumulator  thereby  provides  an  elastic  element  in  the  system, 
which  will  maintain  a  constant  supply  to  the  presses,  acting  as 
a  cushion  against  shocks,  and  giving  the  pump  an  opportunity 
to  get  in  motion  before  there  is  any  marked  drop  in  pressure. 


Fig.  143. 
Sketch  Showing  Accumulator  and  Hydraulic  Pressure  Pump. 


The  accumulator  consists  of  a  vertical  cylinder,  the  upper 
end  of  which  is  provided  with  a  stuffing  box  through  which  a 
plunger  or  ram  works.  This  ram  carries  a  platen  loaded  with 
heavy  weights,  which  are  equivalent  to  the  area  of  the  ram  or 
plunger  multiplied  by  the  water  pressure. 

Figure  143  illustrates  an  accumulator  and  a  hydraulic 
pump.  The  governing  device  which  operates  the  pump  is  so 
arranged  that  the  pump  will  maintain  the  ram  at  its  highest 
position.  The  steam  line  to  the  pump  is  fitted  with  a  butter- 
fly valve,  which  is  operated  by  a  bal- 
anced lever.  When  the  ram  reaches  its 
highest  position,  it  trips  the  weight  W, 
which  isconnected  to  the  chronometer  valve, 
and  stops  the  pump.  When  the  demand 
for  water  increases,  the  ram  descends,  and 
with  it  the  weight  W,  starting  up  the  pump. 

Deep  Well  Pumps 

Figure  144  illustrates  the  type  of  pump 
used  for  non-flowing  artesian,  tubular,  or 
bored  wells,  and  for  dug  or  driven  wells, 
where  the  water  does  not  rise  to  a  sufficient 
height  for  the  ordinary  suction  pump. 

The  working  barrel  connected  to  the  well 
engine  consists  of  a  bronze  cylinder  fitted 
with  a  cup  leather  plunger,  and  ball  valves. 
The  cylinder,  which  is  single  acting,  is  con- 
nected to  the  engine  bed  by  means  of  a  drop 
pipe,  the  flange  of  which  is  bolted  to  the 
discharge  box.  The  plunger  is  generally 
driven  by  means  of  wooden  rods  made  up 
in  sections  coupled  together. 

When  the  deep  well  pump  discharges  into 
an  elevated  tank,  in  order  to   secure    uni- 
form   discharge   from  the  well,  a  displace- 
ment plunger    is   generally    used,    which 
works  through  a  stuffiing   box.     The    dis- 
placement plunger  should  be    made    one- 
Fig.  144  natf    tne    area   °f    tne    weH    plunger    to 
Deep  Well  Pump.      secure  uniform  discharge. 


342 


BATTLE 


C  R  E  E  K 


MJLSJjyg. AN .     U.  S^A 


Milk  Pumps 

For  handling  milk  and  other  liquid  food  products,  it  is 
imperative  that  a  strictly  sanitary  type  .of  pump  should  be  used, 
figure  145a  illustrates  a  direct  acting  milk  pump.  Figure 
145b  shows  the  construction  of  the  liquor  end. 


Fig.  145a 
Sanitary  Pump. 


Fig.  145b 
Section  of  Milk  End  of  Sanitary  Pump. 

The  milk  end  is  a  straight,  smooth,  tubular  cylinder  with 
no  hidden  parts,  or  inaccessible  corners.  The  outer  head  is 
removable  by  turning  four  thumb  nuts.  The  liquor  piston, 
which  is  cast  in  the  form  of  the  letter  H  is  machined  to  fit 
the  bore  of  the  cylinder.  The  ports  are  machined  through  the 
sides  of  the  piston,  and  over  each  part  is  mounted  a  round  flat- 
faced  hinged  valve.  If  it  is  desired  to  remove  the  valves,  it  is 
only  necessary  to  remove  the  pins  on  which  they  swing. 

This  pump  is  so  constructed  that  it  can  be  thoroughly 
cleaned  in  a  few  minuces  time,  as  it  is  only  necessary  to  remove 
one  bolt  from  the  crosshead.  The  entire  assembled  piston  and 
valves  can  then  be  removed,  and  immersed  in  water. 


AND    CONDENSERS    FOR   EVERY  SERVICE 


343 


UNION       S  T  E  AM       PUMP       COMPANY 


Magma  Pumps 

This  type  of  pump  is  designed  for  handling  thick  and 
heavy  liquids,  such  as  massecuite,  etc.  The  liquor  cylinder  is 
made  without  suction  valves,  and  the  material  flows  by  gravity 
into  the  cylinder  through  a  rectangular  port. 

The  discharge  takes  place  at  both  ends  of  the  cylinder 
through  large  flat  faced  valves,  having  free  opening  seats. 
These  valves  are  located  on  the  side  of  the  cylinder,  and  they  are 
easily  accessible  by  the  removal  of  the  hand  plates. 

Figure  146a  illustrates  the  direct  acting  magma  pump, 
and  figure  146b  shows  the  construction  of  the  liquor  cylinder. 


Fig.  146a 
Magma  Pump. 


Fig.  146b 
Section  through  Magma  Cylinder.. 


Oil  Pumps 

Direct  acting  pumps  are  extensively  used  for  handling  oil. 

For  pipe  line  work,  the  pot  valve  plunger  pump  is  generally 
used,  as  the  friction  head  which  this  class  of  pump  operates 
against  is  generally  around  500  to  1000  Ibs.  per  square  inch. 

In  oil  refineries,  etc.,  for  handling  cold  oil,  the  piston  or 
plunger  pump  is  used.  For  this  service,  the  pump  is  generally 
brass  fitted,  and  the  piston  packed  pump  is  fitted  with  ring 
packing,  or  cup  leathers,  as  illustrated  on  page  312. 


344 


jj        BATTLE 

C 

RE 

EK. 

M 

1C 

HIG 

AN. 

U. 

S. 

A. 

Jl 

Pumps  for  handling  hot  oil  in  refineries  may  be  of  the 
piston  or  plunger  type.  Where  the  temperature  of  the  oil  does  not 
exceed  300°  .  a  regular  fitted  pump  is  used.  Piston  pumps 
for  this  service  are  fitted  with  brass  ring  piston  packing. 

For  handling  oil  of  temperatures  from  300  to  800°  .,  the 
pump  should  be  all  iron  fitted,  the  piston  pump  should  be 
fitted  with  ring  packing,  and  the  stuffing  boxes  should  be  packed 
with  asbestos  packing. 

Direct  Acting  Air  Compressors 

This  type  of  compressor  is  used  for  low  pressures  up  to  40 
Ibs.,  where  economy  of  operation  is  not  essential. 

These  compressors  are  used  for  agitating  liquids,  creating 
vacuum  etc.  Figure  147  illustrates  a  direct  acting  air  com- 
pressor. 

For  higher  air  presstires  than  40  Ibs.,  the  fly  type  air  com- 
pressor fully  described  in  Section  One  is  used. 


Fig.  147 
Direct  Acting  Air  Compressor. 


345 


Data  Required   for  Estimates   for   Direct  Acting 
Steam    Pumps 

When  sending  for  estimates,  please  answer  the  following 
questions : 

1 .  For  what  purpose  is  pump  to  be  used  ? 

2 .  (a)  Capacity  of  pump  in  U.  S.  gallons  per  minute  ? 

(b)  If  the  pump  is  for  vacuum  service,  give  the  number 
of  square  feet  of  radiation,  or  the  number  of  cubic  feet  displace- 
ment per  minute  required? 

(c)  If  the  pump  is  for  use  with  a  condenser,  give  the 
number  of  pounds  of  steam  per  hour  to  be  condensed,  temperature 
of  condensing  water,  the  vacuum  to  be  carried  and  the  type  of 
condenser  ? 

(d)  If  pump  is  for  evaporator,  give  the  nature  of  the 
liquid  to  be  evaporated,  the  quantity  of  liquor  to  be  evaporated 
per  hour,  the  temperature  of  the  condensing  water,  the  vacuum 
under  which  the  liquid  is  to  be  evaporated,  and  the  number  of 
the  effects  in  the  evaporator? 

3.  Total  lift,  including  suction,  discharge,  lift,  and  pipe 
friction  in  feet? 

4.  Length  and  diameter  of  the  suction  pipe? 

5 .  Vertical  distance  from  water  level  to  pump  in  feet  ? 

6.  Number  and  size  of  elbows  in  suction  pipe? 

7.  Length  and  diameter  of  discharge  pipe? 

8.  Vertical  distance  above  pump,  or  against  what  pressure 
is  liquid  to  be  discharged? 

9 .  Number  and  size  of  elbows  in  discharge  pipe  ? 

10 .  Number  and  diameter  of  valves  in  discharge  pipe  ? 

11.  Temperature  of  liquid  in  degrees  Fah.  ? 

12.  Specific  gravity  of  liquid? 

13.  •    Nature  of  liquid  to  be  handled:  fresh  water,  salt  water, 
acidulous,  alkaline,  gritty,  etc.? 

14.  What  is  the  lowest  steam  pressure  to  be  used  at  the 
pump? 

15.  (a)  Will  pump  exhaust  into  the  atmosphere? 

(b)  Will  pump  exhaust  into  a  heater?  (State  whether 
open  or  closed). 

16.  What  pressure  will  pump  exhaust  against.'' 

17.  If  pump  is  to  operate  condensing,  give  the  vacuum  to 
be  carried  on  the  condenser  ? 

18.  Where  is  pump  to  be  located,  on  the  surface,  or  under- 
ground ? 


346 


Data  Required  for  Estimates  for  Deep  Well 
Pumping  Engines 

When  sending  for  estimates,  please  answer  the  following 
questions : 

1.  What  is  the  entire  depth  of  well? 

2.  What  is  the  inside  diameter  of  casing? 

3 .  If  boring  is  reduced,  state  at  what  depth  and  to  what 

diameter? . - 

cased  with. inside  diameter  casing  to  a  depth 

of ..feet;  balance  of  well  cased  with 

inside  diameter  casing. 

4.  Depth  from  surface  to  water  level  when  not  pumping 


5 .  Capacity  of  well  when  pumped ....gallons  per  minute. 

6 .  Depth  from  surface  to  water  level  when  pumped  at  this 
capacity ..— 

7.  Style  and  capacity  of  pump  used 

8.  Elevation  above  surface  to  which  water  is  to  be  raised 


9 .      Horizontal  distance  from  well  to  tank. 

10.  Steam  pressure  carried  at  boiler 

1 1 .  How  far  from  well  is  boiler  located  ?.... 


12.  What  is  the  lowest  steam  pressure  you  want  pump  to 
operate  with? _ 

13.  How  many  gallons  of  water  do  you  require  per  hour? 


14.     Have  you  a  water  cylinder  already  in  well?, 
and  at  what  depth?... 


15.     If  so,  what  is  the  diameter?. 
Length  of  stroke  ? 


AND    CONDENSERS    FOR   EVERY  SERVICE 


UNION       STEAM       PUMP       COMPANY 


Burnham  Horizontal  Piston 


Pattern  Boiler  Feed  or 


Pressure  Pumps 


In  the  sizes  listed  below,  14x8x12  and  smaller  are  suitable  for  a  Maximum  Working  Pres- 
sure of  250  Pounds  of  Steam  and  Water.  Larger  sizes  are  suitable  for  a  Maximum  Work- 
ng  Pressure  of  150  Pounds  Steam  and  Water. 


Size  of  Pump 

Diam.  Pipe  Openings 

Ratings 

For  long  pipe  lines  use 

<u 

. 

|H 

J8 

larger  pipes,  reducing  size 

•g 

§'*S 

Tl 

J 

§ 

T3 

8 

at  the  pump  openings 

1 

03 

£1 

«T) 
2£  £ 

•g-S 

"ojH 

co 

0) 

fe 

|j  u 

°'<s 

VH  ^     D 

1? 

1? 

"o 

"1 

(3 

.2 

g 

1 

tn 

c 

^  S 

ll 

W  C.Q 

6  J3 

8  % 

00 

c3 

jS 

1 

H 

cuEEo 

s! 

S£ 

3 

CO 

3 

1 

CO 

p 

13 
O 

11 

<3s 

w£-ii 

4 

2y2 

5 

1A 

F 

11A 

1M 

.106 

140 

14.8 

62 

5 

3 

6 

2 

1  ^2 

.183 

130 

23.8 

106 

5  /^ 

3^2 

7 

1^ 

% 

2y> 

2 

.291 

120 

35 

147 

6//8 

4 

8 

/€ 

i 

2^/2 

2 

.44 

115 

50.7 

220 

7 

43^ 

10 

M 

i 

3 

2y> 

.688 

108 

74.1 

350 

7 

5 

10 

H 

i 

31A 

3 

.85 

108 

92 

430 

83^ 

5 

10 

13^ 

3 

.85 

108 

92 

430 

53^ 

10 

i 

1  3^ 

3  3^2 

3 

1.02 

108 

111 

520 

10 

6 

12 

1  34 

2 

4 

3 

1.46 

100 

146 

635 

10 

gi^ 

12 

1  34 

2 

4 

3 

1.72 

100 

172 

750 

12 

7 

12 

i  y> 

23^2 

5 

4 

2.00 

100 

200 

870 

12 

12 

1  y^ 

2/^ 

5 

4 

2  29 

100 

229 

1000 

12 

8  2 

12 

iK 

2//2 

5 

4 

2.61 

100 

261 

1135 

14 

8 

12 

2 

23^2 

5 

4 

2.61 

100 

261 

1135 

14 

12 

2 

2/^ 

6 

5 

2.94 

100 

294 

1280 

12 

7 

16 

1  ^ 

2  1^ 

5 

4 

2.66 

75 

200 

1160 

12 

16 

1  3^ 

23/2 

5 

4 

3.05 

75 

229 

1330 

12 

8  2 

16 

l;Hj 

23^ 

5 

4 

3.48 

75 

261 

1510 

14 

8 

16 

2 

23^ 

5 

4 

3.48 

75 

261 

1510 

14 

16 

2 

23^ 

6 

5 

3.93 

75 

294 

1710 

14 

9 

16 

2 

2  \^l 

6 

5 

4.40 

75 

330 

1920 

16 

10 

16 

2 

23^ 

8 

6 

5.44 

75 

400 

2375 

18 

12 

16 

3^2 

8 

6 

7.82 

75 

587 

3400 

20 

14 

16 

2^ 

sy> 

10 

8 

10.66 

75 

800 

4650 

18 

12 

20 

2]A 

3^2 

8 

6 

9.78 

60 

587 

4250 

20 

14 

20 

2]/2 

3^2 

10 

8 

13.32 

60 

800 

5800 

24 

16 

20 

3 

5 

10 

8 

17.40 

60 

1044 

7500 

26 

18 

20 

3 

5 

12 

10 

22.00 

60 

1322 

9600 

30 

20 

24 

3 

5 

14 

12 

32.64 

50 

1632 

14200 

348 


BATTLE      CREEK.     MICHIGAN, 


Burnnam  Vertical  Piston  Pattern 
Boiler  Feed  or  Pressure  Pumps 

300  Pounds  Maximum  Steam  and  Water  Pressure 


Fig.  112a 


Size  ot    Fump 

Diameter  of  Pipe   Openings 

Ratings 

For    long    pipe     lines    use 

larger  pipes,  reducing  size 

o 

at  the  pump   openings 

4J 

u 

h 

•g 

O 

t' 

•3 

•'      "E 

2 

is 

0:2 

U     ^* 

a?  u 

u">> 

to 

o 

• 

c 

1 

Ij 

*1 

•Sf* 

if 

a  a 

"So 

i 

i    3 

o 

D 

4> 

1 

I* 

.  ft  J 

Q^ 

j 

to 

o! 

"3 
O 

Ift  ' 

uS 

ffi  &H    C3 

4 

2K 

5 

K 

K 

\\/2 

IK 

.106 

140 

14.8 

62 

5 

3 

6 

K 

K 

2K 

2 

.183 

130 

23.8 

106 

5  Va 

3K 

7 

K 

K 

2K 

2 

.291 

12*0 

35 

147 

6^i 

4 

8 

K 

1 

3 

2K 

.44 

115 

50.7 

220 

7 

4K 

10 

K 

1 

3 

2K 

.688 

108 

74.1 

350 

85^2 

5 

10 

l 

IK 

3K 

3 

.85 

108 

92 

430 

8 

5 

12 

i 

IK 

3K 

3 

1.01 

100 

.101 

440 

10 

6 

12 

1  r/ 

2 

4 

3 

1.46 

100 

146 

635 

10 

6 

16 

|  r/ 

2 

•4 

3 

1.95 

75 

146 

840 

10 

7 

12 

1  K 

2 

5 

4 

2.00 

100 

200 

870 

12 

7 

12 

IK 

2K 

5 

4 

2.00 

100 

200 

870 

12 

7 

16 

IK 

2K 

5 

4 

2.66 

75 

200 

1160 

12 
12 

7 
8 

18 
12 

IK 
IK 

2K 
2K 

5 

5 

4 
4 

2.99 
2.61 

66% 
100 

200 
261 

1300 
1135 

12 

8 

16 

IK 

2K 

5 

4 

3.48 

75 

261 

1510 

12 

8 

18 

IK 

2K 

5 

4 

3.92 

66% 

261 

1700 

12 

8 

24 

IK 

2K 

5 

4 

5.22 

50 

291 

2280 

14 

8 

12 

2 

2K 

5 

4 

2.61 

100 

261 

1135 

14 

8 

16 

2 

2K 

5 

4 

3.48 

75 

261 

1510 

14 

8 

18 

2 

2K 

5 

4 

3.92 

66% 

261 

1700 

14 

8 

24 

2 

2K 

5 

4 

5.22 

50 

261 

2280 

14 

9 

16 

2 

2K 

6 

5 

4.40 

75 

330 

1920 

14 

9 

18 

2 

2K 

6 

5 

4.95 

66% 

330 

2150 

14 

9 

24 

2 

2K 

6 

5 

6.60 

50 

330 

2870 

16 

10 

16 

2 

2K 

6 

5 

5.44 

75 

400 

2375 

16 

10 

18 

2 

2K 

6 

5 

6.12 

66% 

400 

2670 

16 

10 

24 

2 

2K 

6 

5 

8.16 

50 

400 

3550 

l^W^ 

tftiltf»BitfigyWr-i^^ 


349 


UNION       STEAM       PUMP       COMPANY 


Fig.  113 


Burnham  Automatic  Feed  Pumps 
and  Receivers 

250  pounds  Maximum  Steam   and  Water  Pressure 
Receivers  suitable  for  150  Pounds  Maximum  Pressure 


Size  of  Pump 

Size  of  Openings 

CAPACITY 

1  U-'  '"*  *-*  T-V.  r 

totooOOMOOiCntf*  Diameter  of 
t$!  £\^\  Steam  Cylinder 

u 

•si 
fc'i 

•go 

Is 

1 
& 

"o 

1 

1 

For  long  pipe  lines  use 
larger  pipes,  reducing  size 
at  the  pump  openings 

Gallons  per  Min- 
ute at  Speed 
Recommended 

|! 

ll 

1 

1 

1 

| 

"o 

I 

5 

c  42 
'II 

3  2 
4 

5  2 
6 

7 
8 

5 
6 
7 
8 
10 
10 
12 
12 
12 

y2 
y2 

i 

m 

L 

2 

\cs)  \C<I\C^  \cq 
r4\  r-\r-(\  rn\ 

r-KN<N<MCOCOTt<O»O 

2 
2 

3  2 
3 

4 
4 

2-2' 
2-2' 
2-2' 
2-3' 
2-3' 
2-3' 
2-6' 
2-6' 
2-6' 

8.5 
13.5 
20 
30 
41 
51 
73 
100 
130 

8500 
13500 
20000 
30000 
41000 
51000 
73000 
100000 
130000 

Fig.  114 


350 


Union  Vertical   Duplex   Piston   Pattern   Boiler 
Feed   or   Pressure     Pumps 

200  pounds  Maximum  Steam  and  Water  Pressures 


Openings 

Ratings 

S 

]L 

T3 

cd 

SIZE 

<L» 

a 

CJTJ 

ill 

>>J3  § 

||1 

0 

1 

1 

1 

99 

o,c 

coO.S 

fll 

PQ  ? 

rt 

r* 

^1 

u 

SO 

K'o  u 

H*"* 

I 

S 

a 

CO 

a 

rt  rt 

CM 

SiSS, 

c?ST| 

W^rt 

4Kx2^x4 

K 

M 

2 

IK 

.103 

150 

30 

125 

5  Mx3  KX5 

X 

1-8 

2K 

IK 

.208 

140 

58 

300 

6    x4     x6 

IX 

3 

2 

.326 

130 

84 

400 

7Kx5    x6 

IK 

2 

4 

3 

.510 

130 

133 

600 

7Kx4Kxlt 

IK 

2 

4 

3 

.689 

96 

132 

700 

9     x5MxlO 

2 

2K 

4 

3 

.938 

96 

180 

850 

10     x6     xlO 

2 

5 

4 

1.224 

96 

235 

1200 

10     x7     xlO 

2 

2K 

6 

5 

1.66 

96 

318 

1500 

Fig.  103a 

Union  Horizontal  Duplex  Piston   Pattern  Boiler 
Feed  or  Pressure  Pumps 

250  Pounds  Maximum  Steam  Pressure,  259  Pounds  Maximum  Water 
Pressure. 


Diam.  Pump  Openings 

Platings 

For  long  pipe  lines  use  larger 

|                pump  openings 

^ 

<8  *& 

u 

V 

<D    *O 

£    v    ii 

SIZE 

«-.       M 

M    C    u 

c  "^ 

<D  *4~t    9^ 

T-5       ,-H         ft 

S 

ft   W 

£  'f.    3 

K*    r  '^   a> 

•3  ra  co 

+? 

c 

7 

W5              4J 

•^  r^  c 

•tJ  S  o  to 

PQ   ^   fe 

S 

ctf 

1 

.9 

1 

8  4.  i 

^  2'f, 

sft 

i«s  a 

•   ft^ 

G  C/2 

*> 

W 

en 

p 

OcoO 

S  W    ft 

o  d  n  ^ 

W  a*  "S 

2Kx  IKx  3 

3// 

K 

1 

34 

.023 

160 

7.36 

40 

3x2x3 

y* 

1M 

1 

.041 

160 

13.1 

70 

4Kx  2%x  4 

M 

IK 

.103 

150 

30 

150 

5^x  3j/2x  5 

x 

2K 

IK 

.208 

140 

,       58 

250 

6x4x6 

i/4 

3 

2 

.326 

130 

84 

350 

7Kx  5x6 

IK 

2 

4 

3 

.510 

130 

133 

550 

7Kx  5x8 

1  K 

2 

4 

3 

.679 

110 

149 

700 

7Kx  4KxlO 

IK 

2 

4 

3 

.689 

96 

132 

700 

9     x  5^x10 

i  K 

2 

4 

3 

.938 

96 

180 

950 

10     x  6     xlO 

IK 

2 

5 

4 

1.224 

96 

235 

1200 

10     x  6     x!2 

IK 

2 

5 

4 

1.46 

90 

265 

1500 

10     x  7     xlO 

IK 

2 

6 

5 

1.66 

96 

318 

1700 

12     x  7     x!2 

2 

2K 

6 

5 

2.00 

90 

360 

2000 

12     x  8Kxl2 

2 

2K 

6 

5 

2.94 

90 

530 

3000 

14     x  8Kxl2 

2 

2K 

6 

5 

2.94 

90 

530 

3000 

14     xlO     x!2 

2 

2K 

8 

6 

4.08 

90 

730 

4150 

13     xlO     x!2 

2K 

3 

8 

6 

4.08 

90 

730 

4150 

351 


u 

N 

I  0 

N 

ST 

.g>  A  a.  .a.  A  AuLajaLjj 

EAM 

J.jaAjL. 

P 

UM 

BJAiL3_B 
P 

c 

O  M  PANY         | 

Fig.  181 

Union  Duplex  Pressure  Oil  Pumps 

250  Lbs.  Max.  Steam  Pressure.  Max.  Oil  Pressure  Shown  in  Table 


Size  of  Pump 

Diameter  of  Pump 
Openings 

Ratings 

"Q    to 

t5    u 

o 

c 

M 

to 

n          ^ 

d 

<u  O 

S.I 

^ 

* 

g 

^        t—  i 

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351 A 


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BATTLE       CREEK.     MICHIGAN. 


Union  Duplex  Oil  Pumps 

Separate-Chest  Pattern. 
200  Pounds  Maximum  Steam  and  Oil  Pressure. 


Size  of  Pump 

Diameter  of  Pump  Openings 

Ratings 

0 

o 

<u 

M 

<u 

1     *« 

42 

7  % 

Diamett 
Steam  C 

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50 

1174 

1677 

16 

14 

24                3 

4 

14 

10 

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50 

1600 

2285 

Pig.  183 


Union  Duplex  Automatic  Feed  Pumps 
and  Receivers 

250  Lbs.  Maximum  Steam  Pressure.       250  Lbs.  Maximum  Water  Pressure. 
Receivers  suitable  for  150  Lbs.  Maximum  Pressure. 


Size  of  Pump 

Diameter  of  Pump  Openings 

Ratings 

" 

For  long  pipe  lines,  use  larger  pipes 

. 

g 

1 

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300000 

351  B 


Burnham   Horizontal    Outside 
Center-Packed  Plunger  Pumps 


Fig.  105a. 


250  Pounds  Max- 
imum Steam  and 
Water  Pressures 


Size  of  Pump 

Diam.  Pump  Openings 

RATINGS 

q> 

For  long  pipe  lines  use 
larger  pipes,  reducing 

0 

1 

11 

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size  at  pump  openings 

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18 

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12 

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1320 

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26 

18 

24 

3 

5 

12 

10 

26.42 

50 

1320 

11500 

30 

20 

24 

4 

6 

14 

12 

32.64 

50 

1632 

14200 

Pig.  107a 


BATTLE       C  REEK 


G  AN,      U.  S.  A. 


Burnham  Horizontal  Outside  End  Packed 
Plunger  Pumps 

In  the  sizes  listed  below,  the  14x8x  12  and  smaller  are  suitable  for  a 
Maximum  Working  Pressure  of  250  Pounds  Steam  and  Water.  Larger 
size  sare  suitable  for  a  Maximum  Working  Pressure  of -150  Pounds  Steam 
and  Water. 


Size  of  Pump 

Diam.  Pump  Openings 

RATINGS 

For  long  pipe  lines  use 

w 

w 

W-O 

j£ 

larger  pipes,  reducing 

B 

3   Q) 

rt 

y 
<u 

•o 

w 

0) 

§ 

size  at  pump  openings 

02 

| 

jj-jpj 

'o'S 

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C/3 

"to 

G 

0) 

M 

i 

If 

0)   3 

i 

U<    QJ 

III 

S  ^ 

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60 

C 

0) 

1 

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1 

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J 

CO 

w 

01 

Q 

O 

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140 

14.8 

62 

5 

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2 

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7 

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35 

147 

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50.7 

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5 

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108 

92 

430 

10 

6 

12 

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2 

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3 

1.46 

100 

146 

635 

12 

7 

12 

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5 

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2.00 

100 

200 

870 

12 

8 

12 

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2.61 

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2.61 

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261 

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8 

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1510 

14 

8 

16 

2 

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6 

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1510 

14 

9 

16 

2 

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6 

5 

4.40 

75 

-  330 

1920 

16 

10 

16 

2 

2/i 

8 

6 

5.44 

75 

400 

2375 

18 

12 

16 

2  1/2 

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8 

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7.82 

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3400 

20 

14 

16 

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31^ 

10 

8 

10.66 

75 

800 

4650 

24 

16 

20 

3 

5 

10 

8 

17.40 

60 

1044 

7500 

26 

18 

20 

3 

5 

12 

10 

22.00 

60 

1320 

9600 

Fig    109a 
Pot-Valve  Plunger  Pump. 


AND    CONDENSERS    FOR    EVERY  SERVICE 


353 


u 

N 

I  O 

N 

ST 

E  AM 

P 

UM 

P 

CO 

M  PANV         | 

Burnham  Horizontal  Outside  End  Packed 
Pot  Valve  Plunger  Pumps 

250  Pounds  Maximum  Steam  and  Water  Pressures. 


Size  of  Pump 

Diam.  Pump  Openings 

Ratings 

For  long  pipe  lines  use 

<B 

U-V 

-g 

& 

0) 

1 

larger  pipes,  reducing 
size  at  pump  Openings 

1 

1 

"tj  a> 

14 

•old 

•a 

•a 

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C/2 

£ 

r=H  rl 

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m  c 

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w 
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1 

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w 

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s 

0 

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3 

7 

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^ 

23/9 

2 

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120 

25.7 

105 

5H 

7 

H 

M 

2^/2 

2 

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120 

35 

147 

6^i 

4  2 

8 

l 

2  1^ 

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115 

50.6 

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1.46 

100 

146 

635 

12 

7 

16 

1^2 

22/4 

5 

4 

2.66 

75 

200 

11C3 

12 

7/^ 

16 

1M 

2/i 

5 

4 

3.05 

75 

229 

1330 

14 

8 

16 

2 

2^ 

6 

5 

3.48 

75 

261 

1510 

14 

9 

16 

2 

2M 

6 

5 

4.40 

75 

330 

1920 

16 

10 

16 

2 

2y. 

8 

6 

5.44 

75 

400 

2375 

16 

10  H 

16 

2 

2y 

8 

6 

6.00 

75 

450 

2600 

16 

10 

20 

2 

2J9 

8 

6 

6.80 

60 

400 

2950 

16 

10  J^ 

20 

2 

2^ 

8 

6 

7.49 

6" 

450 

3250 

Union  Horizontal 

Duplex  Outside  End 

Packed    Pot  Valve 

Plunger  Pumps 

250  Pounds  Max.  Steam  Pressure, 
300  Pounds  Max.  Water  Pressure. 


Fig.  203. 


Size  of  Pump 

Diam.  Pump  Openings 

Ratings 

For  long  pipe  lines  use 

jj 

^ 

b 

larger  pipes,  reducing 

0 

fj 

J 

| 

size  at  pump  openings 

^-S 

£      o> 

1 

Bj 

«a 

«3  S 

<u  G 

«  -^  c 

%  6.2 

11 

If 

o 

4s 

- 

1 

c 
o 

• 
& 

go 

jjj 

^3 

{}*! 

i| 

.2  "S 

c  S 

1 

1 

o 

9 

5 

ow 

.sal 

oil 

6 

4 

6 

1 

l1^ 

3 

2 

.326 

130 

84 

350 

10 

2 

4 

3 

.689 

96 

132 

700 

9 

5 

10 

\\/ 

2 

4 

3 

.819 

96 

163 

860 

10 

5 

10 

ivl 

2 

4 

3 

.849 

96 

163 

860 

10 

6 

12 

1"H 

2 

5 

4 

1.46 

90 

265 

1500 

6 

12 

2 

2H 

5 

4 

1.46 

90 

265 

1500 

12 

7 

12 

2 

2/'2 

6 

5 

2.00 

90 

360 

2000 

14 

7 

12 

2 

23^ 

6 

5 

2.00 

90 

360 

2000 

«*"*»»  «I_B  «Alj« « M  * « *  » aaegjaaggBKa-BJuiM-* a  B  «  a  «  a  a B  njj 


Burnham  Compound   Steam  Pumps 


Fig.  117. 


Heavy  Service  Piston  Pattern 

250  Pounds  Maximum  Steam  and  Water  Pressures  for  first  five  sizes. 
200  Pounds  Maximum  Steam,  150  Pounds  Maximum  Water  Pressures  larger 


Size  of  Pump 

Diam.  Pump  Openings 

Ratings 

For  long  pipe  lines  use 

j£ 

larger  pipes,  reducing  size 

a 

*S 

•si! 

•s§i 

"S-S 

a 

CO 

at.  the  purnp  openings 

a 

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Diameter 
High-Pres 
Steam  Cy] 

Diameter 
Low-Press 
Steam  Cyl 

Diameter 
Water  Cy 

Length  of 

6 

CO 

Exhaust 

Suction 

Discharge 

||| 

Gallons  pi 
Minute  at 
feet  Pisto 

ill 

8 

12 

6 

12 

1 

2ft 

4 

3 

1.4676 

146 

8812 

8 

12 

7 

12 

1 

23/2 

5 

4 

1.998 

200 

11995 

8 

12 

8 

12 

1 

2  j/2 

5 

4 

2.61 

261 

15667 

10 

16 

9 

16 

1  M 

2^2 

6 

5 

4.4048 

330 

19828 

10 

16 

10 

16 

l  M 

%y> 

8 

6 

5.44 

408 

24480 

12 

18 

9 

16 

13/2 

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6 

5 

4.4048 

330 

19828 

12 

18 

10 

16 

1  3/2 

3/4 

8 

6 

5.44 

408 

24480 

12 

18 

12 

16 

1  % 

3/4 

8 

6 

7.8272 

587 

35251 

12 

18 

14 

16 

1  ^2 

33/2 

10 

8 

10.6592 

799 

47980 

12 

18 

14 

20 

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3H 

10 

8 

13.324 

799 

47980 

14 

20 

10 

16 

2 

3/4 

8 

6 

5.44 

408 

24480 

14 

20 

12 

16 

2 

33/2 

8 

6 

7.8272 

587 

35251 

14 

20 

14 

16 

2 

33^ 

10 

8 

10.6592 

799 

47980 

14 

20 

14 

20 

2 

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10 

8 

13.324 

799 

47980 

14 

20 

16 

20 

2 

3/4 

12 

10 

17.4 

1044 

62668 

16 

24 

12 

16 

2 

5 

10 

8 

7  8272 

587 

35251 

16 

24 

14 

16 

2 

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10 

8 

10.6592 

799 

47980 

16 

24 

14 

20 

2 

5 

10 

8 

13.324 

799 

47980 

16 

24 

16 

20 

2 

5 

12 

10 

17.4 

1044 

62668 

16 

24 

18 

20 

2 

5 

12 

10 

22.024 

1322 

79314 

18 

26 

14 

16 

21/2' 

5 

10 

8 

1  0.6592 

799 

47980 

18 

26 

14 

20 

23/2" 

5 

10 

8 

13.324 

799 

47980 

18 

26 

16 

20 

23/2' 

5 

12 

10 

17.4 

1044 

62668 

18 

26 

18 

20 

23/2 

5 

12 

10 

22.024 

1322 

79314 

18 

26 

20 

24 

2^2 

5 

14 

12 

32.64 

1.632 

97920 

20 

30 

16 

20 

2  3-^ 

5 

12 

10 

17.4 

1044 

62668 

20 

30 

18 

20 

2^2 

5 

12 

10 

22.024 

1322 

79314 

20 

30 

20 

24 

2/4 

6 

14 

12 

32.64 

1632 

97920 

24 

36 

16 

20 

3 

6 

12 

10 

17.4 

1044 

62668 

24 

36 

18 

20 

3 

6 

12 

10 

22  024 

1322 

79314 

24 

36 

20 

24 

3 

6 

14 

12 

32.64 

1T32 

97920 

AND    CONDENSERS    FOR    EVERY   SERVICE 


355 


UNION       STEAM       PUMP       COM  P  ANY 


Burnham  Compound  Steam  Pumps 

Light  Service  Piston  Pattern. 
Pig.  149 


200  Pounds  Max- 
imum Steam  Pres- 
sure, 100  Pounds 
Maximum  Water 
Pressure,  12  inch 
stroke  and  smaller, 
75  Ibs.  Maximum. 
Water  Pressure  for 
larger  sizes. 


Size  of  Pump 

Diam.  Pump  Openings 

Ratings 

''or  long  pipe  lines  use 

0)  C 

0) 

arger  pipes,  reducing  size 

& 

,_ 

£  a 

>5S 

CD 

p 

at  the  pump  openings 

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J| 

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1.22 

146 

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5 

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7 

10 

H 

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5 

4 

1.665 

200 

11995 

5 

8K 

8 

10 

1  K 

5 

4 

2.175 

261 

15667 

5 

8K 

10 

10 

H 

IK 

6 

5 

3.40 

408 

24480 

6H 

8K 

7 

10 

H 

IK 

5 

4 

1.665 

200 

11995 

6l/s 

8K 

8 

10 

H 

IK 

5 

4 

2.175 

261 

15667 

QYs 

8K 

10 

10 

H 

IK 

6 

5 

3.40 

408 

24480 

8 

12 

10 

12 

2K 

8 

6 

4.08 

408 

24480 

8 

12 

12 

16 

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2K 

8 

6 

7.82 

587 

35251 

8 

12 

14 

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Fig.  150 
Burnham  Compound  Steam  Pumps 

Outside-Center-Packed  Plunger  Pattern 

200  Pounds  Maximum  Steam  Pressure,  250  Pounds  Maximum  Water 
Pressure. 


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Ratings 

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fli 

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Fig.  151 

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Outside  End-Packed  Plunger  Pattern 

250  Pounds  Maximum  Steam  and  Water  Pressures  for  12  inch  stroke 
pumps,  150  Pounds  Maximum  Steam  and  Water  Pressures  for  larger  sizes 


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358 


Burnham  Compound  Steam  Pumps 

Outside  End-Packed  Pot  Valve  Plunger  Pattern 


250  Pounds  Max- 
imum Steam,  and 
Water  Pressures. 


Fig.  152 


Size  of  Pump 

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o 

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359 


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2K 

3K 

15 

12 

39.48 

50 

1974 

118440 

18 

24 

24 

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3K 

16 

14 

46.99 

50 

2350 

141000 

20 

16 

20 

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3K 

10 

8 

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1044 

62640 

20 

18 

20 

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3K 

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10 

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1320 

79200 

20 

20 

24 

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3K 

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12 

32.64 

50 

1632 

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20 

22 

24 

2K 

3K 

15 

12 

39.48 

50 

1974 

118440 

20 

24 

24 

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3K 

16 

14 

46.99 

50 

2350 

141000 

20 

26 

24 

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3K 

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16 

55.15 

50 

2757 

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28 

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3K 

18 

16 

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50 

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24 

24 

24 

3 

5 

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14 

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50 

2350 

141000 

24 

26 

24 

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5 

18 

16 

55.15 

50 

2757 

165420 

24 

28 

24 

3 

5 

18 

16 

63.96 

50 

3198 

191880 

AND    CONDENSERS    FOR    EVERY  SERVICE 


i         UNION 

STEAM 

P  UM  P 

COM  PANY 

"1 

Burnham  Vertical 
Light-Service 
Piston  Pumps 


200  Pounds  Maximum  Steam 

Pressure,  100  Pounds 

Maximum   Water 

Pressure. 


Fig.  112a 


Size  of    Pump 

Diam.  Pump  Openings 

Ratings 

For  long  pipe  lines  use 

larger  pipes,  reducing  size 

<u 

0) 

tu 

£ 

*o 

u 

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1 

at  the  pump  openings 

1 

c 
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6 

5 

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10 

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2 

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5.44 

75 

408 

24480 

362 


B  ATTLE 

C 

RE 

E 

K. 

M 

ICH 

1G 

AN. 

U. 

S. 

Fig.  102a 


Union    Horizontal   Duplex   Light   Service    Piston 

Pumps 

250  Pounds  Maximum  Steam  Pressure,  125  Pounds  Maximum  Water 
Pressure. 


Diam.  of  Pump  Openings 

Ratings 

For  long  pipe  lines  use  larger  pipes, 

reducing  size  at  the  pump  openings' 

1  • 

SIZE 

. 

& 

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c/2"*1"1  0 

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2 

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10 

8 

5.87 

90 

1058 

16     X12     x!2 

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3 

10 

8 

5.87 

90 

1058 

Fig.  114 


AND   CONDENSERS    FOR   EVERY  SERVICE 


363 


c 

U  N 

I  O 

N 

STE 

AM 

P 

UM 

P 

CO 

MPANY 

3 

Union  Vertical  Duplex  Light  Service  Piston 

Pumps 

200    Pounds     Maximum    Steam    Pressure,   100      Pounds    Maximum 
Water  Pressure. 


OPENINGS 

Ratings 

SIZE 

1. 

£ 

"w 

§ 

w      ^ 

£_£*>> 

"•%& 

1 

3 

.2 

d 

0-^^! 

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3 

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150 
140 

57 
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2 

8 

7 

3.57 

108 

775 

10    x!2     x!2 

2 

2K 

8 

7 

5.89 

90 

1050 

Fig.  134 


364 


Burnham  Horizontal  Mine  Pumps   (Fig.  135) 

200  Pounds  Maximum  Steam  Pressure,  150  Pounds  Maximum  Water 
Pressure. 


Size  of  Pump 

Diam.  of  Pump   Openings 

Ratings 

0> 

For  long  pipe  lines  use 

V 

~c£ 

Lt 

01 

V 

o 

larger  pipes,  reducing  size 

•g 

c  °  3 

•si 

•si 

to 

at  the  pump  openings 

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1 

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2 

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50 

3000 

6 

4 

7 

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2 

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65 

3900 

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3K 

7 

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7 

4 

7 

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2K 

2 

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3K 

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4 

12 

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3 

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8 

5 

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6 

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5 

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3 

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7 

13 

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5 

4 

2.16 

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12000 

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7 

13 

2 

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4 

2.16 

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12000 

14 

8 

13 

2 

2K 

6 

5 

2.82 

260 

15600 

14 

8 

24 

2 

2K 

6 

5 

5.22 

260 

15600 

14 

9 

18 

2 

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5 

4.95 

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16 

9 

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6 

5 

4.95 

331  . 

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16 

10 

18 

2 

2K 

8 

6 

6.12 

410 

24600 

16 

10K 

18 

2 

2K 

8 

6 

6.74 

451 

27060 

18 

10K 

18 

2K 

3K 

8 

6 

6.74 

451 

27060 

Burnham  Vertical  Sinking  Pumps    (Fig.  134) 

200  Pounds  Maximum  Steam  Pressure,  1 50  Pounds  Maximum  Wat  e 
Pressure. 


Size  of  Pump 

Diameter  of  Pump 

Ratings 

wpenmgs 

For  long  pipe  lines  use 

S 

larger  pipes,  reducing 

•g 

§ 

•§ 

size  at  pump  openings 

c 

H 

V 
T) 

0 

8 

9 

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7 

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7 

4 

12 

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65 

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3K 

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4 

12 

1 

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3 

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65 

3900 

10 

5 

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2K 

4 

3 

1.10 

100 

6000 

10 

6 

13 

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4 

3K 

1.58 

150 

9000 

12 

5 

13 

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2K 

4 

3 

1.10 

100 

6000 

12 

6 

13 

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2K 

4 

3K 

1.58 

150 

9000 

12 

7 

13 

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2K 

5 

4 

2.16 

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12000 

14 

7 

13 

2 

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5 

4 

2.16 

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8 

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2 

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5 

2.82 

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2 

2K 

6 

5 

3.19 

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17688 

16 

8 

16 

2 

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6 

5 

3.48 

261 

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16 

8K 

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2 

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17688 

AND    CON D E N  S  E RS    FOR    EVE RV  S  ERVICE 


365 


Fig.  141a 
Low  Vacuum  Pump 

Burnham  Horizontal  Low  Vacuum  Pumps 

Standard  Pattern — Cast-Yoke  Pumps 

200  Pounds  Maximum  Steam  Pressure,  20  inch  Vacuum  with  30  inch 
Barometer. 


Size  of  Pump 

Ratings 

SIZE  OF  OPENINGS 

<D 

For  long  pipe  lines  use 

i 

cj 

larger  pipes,  reducingfsize 

S 

E 

•o 

<~\i 

'Z'JZ   4> 

at  the  pump  openings 

"o.S 

..  r  rt 
o-S 

.pC/3 

S  ^   O  0) 

Diameter 
Steam  Cyl 

Diameter  ( 
Water  Cyl 

SI 

h 

il 

3^ 
&& 

1! 

jj 

Exhaust 

Suction 

Discharge 

3 

3K 

4 

2000 

16 

y* 

K 

2 

IK 

3 

4 

4 

2500 

21 

y% 

2 

i  y> 

4 

5 

2500 

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2 

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4 

4  2 

5 

3500 

27 

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5 

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5000 

42 

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6 

4000 

32 

2 

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8000 

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5 

6 

10 

13000 

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7 

10 

19000 

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3 

5 

8 

10 

25000 

217 

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% 

4 

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5 

8 

12 

33000 

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% 

4 

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6 

7 

10000 

85 

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3 

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l 

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366 


BATTLE      CREEK.     MICHIGAN, 


Burnham  Horizontal  Low  Vacuum  Pumps 
(Continued) 

Standard  Pattern — Cast-Yoke  Pumps 

200  Pounds  Maximum  Steam  Pressure,  20  inch  Vacuum  with  30  inch 
Barometer. 


Size  of  Pump 

Ratings 

Size  of  Openings 

For  long  pipe  lines  use 

larger  pipes,  reducing 

U 

c  a 

at  the  pump  openings 

1 

"o 

I  - 

"o 
w, 

4>         (M 

CO 

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fill 

§ 

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Pig.  141 


367 


UNION       STEAM       PUMP       COMPANY 


Burnham  Horizontal  Low  Vacuum  Pumps 

Standard  Pattern— Rod-Yoke  Pumps 

200  Pounds  Maximum  Steam  Pressure,  20  inch  Vacuum  with  30  inch 
Barometer. 


Size  of  Pump 

Ratings 

Size  of  Openings 

4) 

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u 

Q 

O 

*"^  *H  m 

larger  pipes,  reducing  size 

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1  n-i  a> 

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10 

14 

20 

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1330 

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7 

6 

12 

14 

20 

112000 

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7 

6 

12 
12 

16 

18 

20 
20 

135000 
185000 

1740 
2200 

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8 
10 

6 
8 

14 

14 

20 

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1330 

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6 

14 

16 

20 

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2 

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8 

6 

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18 

20 

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8 

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20 

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10 

S 

f  Fig.  89 

Burnham  Horizontal  High  Vacuum  Pumps 

Standard  Pattern — Cast-Yoke  Pumps 

200  Pounds  Maximum   Steam  Pressure,    26   inch  Vacuum    with  30 
inch  Barometer. 


Size  of  Pump 

Ratings 

Size  of  Openings 

^ 

For  long  pipe  lines  use 

3 

larger  pipes,  reducing  size 

« 

ts 

o 

.S^n 

.at  the  pump  openings 

*o 

*o 

c 

-g.S  a 

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2 

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368 


B  A T1*LE__C _R.E  E  K .     MIC  H  I  G  AN,      U    S .  A 


Burnham  Horizontal  High  Vacuum  Pumps 
(Continued) 

Standard  Pattern — Cast-Yoke  Pumps 

200  Pounds  Maximum  Steam    Pressure,     26  inch  Vacuum  with  30 
inch  Barometer. 


Size  of  Pump 

Ratings 

Size  of  Openings 

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Fig.  155 


Burnham  Horizontal  High-Vacuum  Pumps 

Standard  Pattern — Rod-Yoke  Pumps 

200  Pounds    Maximum    Steam  Pressure,    26  inch  Vacuum   with    30 
inch  Barometer. 


Size  of  Pump 

Ratings 

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Burnham  Horizontal  High- Vacuum  Pumps 

Inverted  Suction-Valve  Design 

200  Pounds  Maximum  Steam  Pressure,  28  inch  Vacuum  with  30  inch 
Barometer. 


Size  of  Pump 

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AND    CONDENSERS    FOR   EVERY  SERVICE 


371 


Burnham  Vertical  Vacuum  Pumps 


Burnham  Vertical  High 
Vacuum  Pumps.  200 
Pounds  Maximum  Steam 
Pressure,  26  inch  Vacuum 
with  30  inch  Barometer. 


Fig.  156 


Size  of  Pump 

Ratings 

Size  of  Openings 

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Burnham  Hydraulic- Pressure  Pumps 

With  Cast-Iron  Water  Cylinders 


200  Pounds  Maximum    Steam    Pressure, 
Water  Pressure. 


2000    Pounds     Maximum 


Size  of   Pump 


Diameter  of  Pipe 


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3 

2 

60 

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Fig.  Ilia 


Burnham  Hydraulic- Pressure  Pumps 

With  Forged-Steel  Water  Cylinder 

200  Pounds  Maximum  Steam  Pressure,  5000  Pounds  Maximum  Water 
Pressure. 


Size  of  Pump 


Diameter  Pipe  Openings 


Ratings 


Diameter  of 
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Diameter  of 
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Length  of 
Stroke 

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larger  pipes,  reducing  size 
at  the  pump  openings 

8, 

(2   D 

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Balanced  Pres- 
sure at  85 
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1 

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200  Pounds  Maximum  Steam  Pressure. 


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AND    CONDENSERS    FOR    EVERY  SERVICE 


Burnham  Air  Compressors— Continued 

200  Pounds  Maximum  Steam  Pressure 


Size  of  Compresso 

Diam.  of  Compressor 
Openings 

Ratings 

For   long  pipe    lines    us 

V 

larger  pipes,  reducing  siz 

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12 

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78 

100 

45  Ibs. 

14 

12 

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23/9 

.785 

78 

100 

60  Ibs. 

10 

14 

16 

1  y 

2 

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1.42 

114 

80 

22  Ibs. 

10 

16 

16 

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1.86 

148 

80 

17  Ibs. 

12 

14 

16 

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4 

1.42 

114 

80 

33  Ibs. 

12 

16 

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1/4 

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1.86 

148 

80 

24  Ibs. 

14 

14 

16 

2 

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1.42 

114 

80 

45  Ibs. 

14 

16 

16 

2 

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1.86 

148 

80 

33  Ibs. 

16 

14 

16 

2 

23^ 

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1.42 

114 

80 

60  Ibs. 

16 

16 

16 

2 

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4 

1.86 

148 

80 

45  Ibs. 

18 

16 

16 

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3H 

43^ 

4 

1.86 

48 

80 

55  Ibs. 

20 

16 

16 

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1.86 

48 

80 

70  Ibs. 

14 

18 

20 

2 

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2.94 

76 

60 

27  Ibs. 

14 

20 

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3.63 

218 

60 

22  Ibs. 

16 

18 

20 

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2.94 

76 

60 

35  Ibs. 

16 

20 

20 

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3.63 

18 

60 

29  Ibs. 

18 

18 

20 

2-Hz 

33^ 

6 

41^ 

2.94 

76 

60 

45  Ibs. 

18 

20 

20 

2/^ 

31^ 

6 

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3.63 

18 

60 

35  Ibs. 

20 

18 

20. 

2/^ 

31^ 

6 

43^ 

2.94 

76 

60 

55  Ibs. 

20 

20 

20 

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33^ 

6 

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3.63 

18 

60 

45  Ibs. 

16 

22 

24 

2 

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6 

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5.27 

63 

50 

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24 

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20  Ibs. 

18 

22 

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63 

50 

30  Ibs. 

18 

24 

24 

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6 

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6.28 

314 

50 

25  Ibs. 

Fig.  157. 


PU MP  IN G    M  A  C  H I N  E  RY,    AIR 


376 


BATTLE      CR  E  E  K .     M  I C  HI  CAN .      U.  S.  A. 

pgaflny-g^iraTrwwgg^fl^WYy  a  g^vvtt  tt\i  tttt  w^ni^-1^  «u»  g tf- 


Burnham  Deep-Well  Pumping  Engines 

150  Pounds  Maximum  Steam  Pressure 


Size  of  Engine 

Diameter  of  Engine  openings 

T3 

For  Long  Pipe  Lines  use  Larger  Pipes, 
Reducing  Size  at  the    Engine    Openings 

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Fig.  146a 


S  T  E  AM       P  U  M  P       COM  P  ANY 


Burnham  Magma  Pumps 

200  Pounds  Maximum  Steam  Pressure.    75  Pounds  Maximum  Liquid  Pressure 


Size  of  Pump 


Size  of  Openings 


Ratings 


For  long  pipe  lines  use 

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larger  pipes,  reducing 

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20 

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6.79 

204 

*The  actual  amount  of  liquor    handled  with  a  magma  pump  is  60%  of  its  piston 
displacement. 


Burnham  Sanitary  Milk  Pumps. 

200  Pounds  Maximum  Steam  Pressure 


Size  of  Pump 

Size  of  Openings 

Ratings 

G 

^4 

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1.06 

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4 

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40-140 

2.30 

4000  to  19000 

5 

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2 

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30-130 

4.32 

7500  to  30000 

6^ 

7 

8 

1 

3 

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30-120 

11.20 

20000to  80000 

378 


JUL 


Power  Pumps 

and 

Crank  and  Fly- 
wheel Pumps 


SECTION  SIX 


P  U  M  P 


Power  Pumps  and  Crank  and  Fly  Wheel  Pumps 

Pumps  operated  through  the  medium  of  a  crank  and  con- 
necting rod  are  classified  as  Power  Pumps,  and  Crank  and  Fly 
Wheel  Pumps. 

Power  Pumps 

Power  Pumps,  as  the  name  indicates  are  generally  operated 
by  the  application  of  power  on  the  crank,  which  is  transmitted 
through  the  connecting  rod,  and  crosshead  to  the  water  piston 
or  plunger. 

Power  Pumps  are  classified  with  respect  to  the  power  and, 
according  to  the  number  of  cranks  into  single,  duplex,  and  tri- 
plex. 


Fig.  158 

Single  Belt  Driven 
Piston  Pump. 


Fig.  206. 
Duplex  Belt- 
Driven 
Piston  ,Pump. 


Fig.  160 

Triplex    Belt 

Driven 
Plunger  Pump. 


PUMPING    MACHINERY    AIR   COMPRESSORS 


380 


Power  Pumps  are  employed  in  localities  where  the  con- 
ditions are  such  that  it  is  more  practical  to  operate  a  pump 
by  belt  or  electricity,  than  to  use  a  steam  driven  direct  acting 
pump. 

Belt  Driven  Power  Pumps  are  generally  back-geared  with 
one  reduction  of  gearing,  the  gears  have  cut  teeth^  and  the 
pinion  is  sometimes  made  of  raw  hide  to  reduce  the  noise. 


Fig.  161 

Plain  Belt  Driven 
Vacuum   Pump. 


Belt  Driven  Pumps  are  divided  into  two  types  viz.  the 
plain  belt  drive,  and  the  short  belt  drive.  The  former,  which 
is  illustrated  in  figure  161  is  operated  by  its  motive  power 
placed  at  a  sufficient  distance  from  same  (usually  three  times 
the  diameter  of  the  driven  pulley)  to  insure  a  liberal  arc  of  con- 
tact on  the  driving  pulley. 


Fig.  162 
Belt    Driven  Vacuum  Pump    Short  Belt  Drive. 

The  short  belt  drive  figure  162  consists  of  a  belt  tightener 
placed  on  the  upper  side  (the  slack  side)  of  the  belt,  which  in- 
creases the  arc  of  contact  on  the  driving  and  driven  pulley,  and 
makes  it  possible  to  place  the  pump,  and  motive  power  very 
close  together.  This  type  of  drive  is  very  compact,  and  is  be- 
ing  used  extensively. 


AND    CONDENSERS    FOR    EVERY  SERVICE 


381 


Fig.  163 

Electric  Gear  Driven 
Piston   Pump 


Electric  gear  driven  power  pumps  are  usually  backgeared 
with  two  reductions  of  gearing.  The  gears  have  cut  teeth,  and 
the  motor  pinion,  and  sometimes  the  gear-shaft  pinion  is  made 
of  raw  hide  to  reduce  the  noise. 


The  type  of  drive  to  employ  is  purely  a  problem  for  the 
user  to  solve,  as  the  local  conditions  are  the  determining  factor. 
The  belt  drive  is  the  most  practical  type  of  drive  for  the  reasons 
that  it  operates  with  a  minimum  amount  of  noise,  and  if  a  sud- 
denly applied  shock  or  excess  pressure  is  put  on  the  water  end, 
it  will  either  throw  the  belt  or  cause  it  to  slip  without  injuring 
the  pump. 


The  belt  drive  is  recommended  for  all  installations  where 
noise  is  obectionable.  There  are  localities  where  the  electric 
gear  driven  pump  is  the  only  type  to  use.  For  instance,  in 
mines  and  facturies,  where  noise  is  not  objectionable,  and  where 
on  account  of  the  moisture,  etc. ,  it  is  not  practical  to  use  the 
belt  drive. 


The  chief  advantage  of  the  electric  gear  drive  is  that  it  is 
very  compact. 


382 


T T  L  E     c BL E'E K . 

* 


Crank  and  Flywheel  Pumps, 


Crank  and  flywhesl  pumps  are  generally  steam  driven, 
and  the  power  is  applied  through  the  steam  piston  and  piston 
rod  to  the  water  piston  or  plunger,  the  reciprocating  action  of 
which  is  transmitted  through  the  crosshead,  and  connecting  rod 
to  the  crank.  In  this  type  of  pump  the  fly  wheels  store  up  the 
energy  during  the  first  half  of  the  stroke,  in  order  to  replenish 
it  during  the  remainder  of  the  stroke,  with  the  result  that  the 
steam  may  be  used  expansively. 


Crank  and  flywheel  pumps  are  classified  with  respect  to 
the  power  end,  according  to  the  number  of  cranks  into  single 
and  duplex  pumps. 


Fig.  91 

Single  Crank  and  Flywheel 
Dry  Vacuum  Pump, 


Fig.   164 

Duplex  Crank  and 

Flywheel 
Wet  Vacuum  Pump 


The  crank  and  flywheel  pump,  on  account  of  being  able  to 
use  the  steam  extensively,  is  used  where  economy  is  of  prime 
importance. 

Power  pumps  and  crank  and  flywheel  pumps  are  classified 
with  respect  to  the  type  of  water  end  into  piston  and  plunger 
pumps. 


AND    CONDENSERS    FOR    EVERY  SERVICE 


383 


Water  End  Classification 

The  different  types  of  water  ends  employed  on  power  and 
crank  and  fly  wheel  pumps  shown  herein,  the  manner  of  fitting 
same  for  different  classes  of  service,  and  in  fact  all  information 
respecting  the  water  end  of  the  pump  is  given  in  Section  Five. 

Efficiency 

In  calculating  the  horse  power  required  to  operate  .  power 
pumps  it  is  necessary  to  take  into  consideration  the  efficiency  of 
the  pump. 

The  efficiency  E  is  the  ratio  of  the  water  horse  power  to 
the  brake  horse  power.  That  is 

Water  Horse   Power 
Brake  Horse  Power 

The  efficiency  of  power  pumps  varies  with  conditions  of  oper- 
ation, and  this  factor  is  obtained  only  from  actual  test. 

The  following  table  gives  the  mechanical  efficiency  of  power 
pumps,  and  for  calculating  purposes  it  is  advisable  to  multiply 
these  figures  by  90%  in  order  to  take  care  of  any  unforeseen 
losses. 

Size  of  Pump  Efficiency 

4"    stroke 
5"       » 
6"       " 
8"       " 
10"       " 
12"       " 
16"        " 
20"       " 

Calculating  the  Horse  Power  to  Operate   Power  Pressure  Pump:; 
To  calculate  the  horse  power  required  to  operate  a  power 
pump  the  theoretical  horse  power  is  first  determined. 

To  calculate  the  theoretical  horse  power  multiply  the  weight 
of  the  liquid  to  be  pumped  per  minute  in  pounds  by  the  total  head 
in  feet  that  it  is  to  be  pumped,  and  divide  this  result  by  33000. 
This  gives  the  following  formula: 
T,        TT   p         Wt.  liquid  per  minute  in  pounds  x  head  in  feet 

33,000 

If  the  liquid  to  be  pumped  is  water,  then  the  formula  for 
horse  power  to  operate  the  power  pump  becomes 

WxH 
33,000  xE 

Where  W=  Weight  of  liquid  pumped  per  minute  in  pounds. 
H=-The  total  head  in  feet. 
E=The  efficiency  of  the  pump. 
For  a  pump  handling  water 


H.  P.  -  -H  xG  (61) 

ll/ 


384 


ir 

B 

ATTL 

E 

CR 

EEK. 

MIC 

H 

IGA 

N,      U. 

S. 

A.        \ 

Where  H=The  total  heat  in  feet. 
G= Gallons  per  minute. 
E=The  efficiency  of  the  pump. 

Example 

It  is  desired  to  elevate  300  gallons  per  minute  of  water  to  an 
elevation  of  200  feet  through  300  lineal  feet  of  4"  pipe  with  three 
90°  elbows,  and  one  4"  globe  valve.  What  horse  power  is  re- 
quired to  operate  a  power  pump  for  this  duty,  assuming  that  it 
has  an  efficiency  of  70%  ? 

The  friction  loss  of  300  gallons  per  minute  through  300  feet 
of  4"  pipe  from  the  table  on  page  145  is  equal  to  18.30  feet.  The 
friction  loss  of  300  gallons  per  minute  through  three  90°  elbows 
from  the  table  on  page  147  is  equal  to  2.658  ^feet.  The  friction 
loss  of  300  gallons  per  minute  through  one  4"  globe  valve  from 
the  table  on  page  148  is  equivalent  to  30  feet  of  4"  pipe,  and  from 
the  table  on  page  145  the  friction  loss  of  300  gallons  per  minute 
through  30  feet  of  4"  pipe— 

04 
6.15  x  T7r7r-=  1.476  feet 

1UU 

The  total  head,  therefore,  is  equivalent  to  the  sum  of  the  above 
heads  or, 

Friction  head  in  pipe  =    18.30' 

11  "     "   elbow  =     2.658' 

"  "     "  valve  =      1.476' 

Static  Head  =  200 ' 


Total  Head  222.434 ' 

Then  the  horse  power  to  operate  the  pump  from  formula  61 
assuming  70%  efficiency  is 

.000252  x  222.434  x  300 

~70~ 

In  selecting  a  motor  to  operate  the  power  pump  it  would  be 
advisable  to  use  a  25  horse  power  motor. 


Horse    Power    to    Operate    Power   Wet   Vacuum 

Pumps 

To  calculate  the  horse  power  to  operate  a  power  wet  vacuum 
pump,  formula  61  may  be  used  by  substitnting  for  H  35  feet 
(which  is  the  equivalent  of  15  Ibs.  pressure),  and  for  G  the  dis- 
placement of  the  pump  in  gallons  per  minute.  The  mechanical 
efficiency  given  on  page  384  is  applicable  to  this  type  of  pump. 

Having  determined  the  horse  power  required,  the  cost  of  op- 
erating the  pump  per  hour  can  be  obtained  by  multiplying  this 
figure  by  the  cost  per  horse  power  hour  of  operating  the  motor  or 
engine  used  to  drive  the  pump. 


r..-vffi-?-.£9ff.P^ 


385 


UN 

I  ON 

STE 

AM 

P 

U  M 

P 

C  O 

M 

PAN 

Y 

3 

Types  of  Motors  to  Use  With  Power  Pumps 

For  power  pumps  we  recommend  for  direct  current  motors 
the  Compound  Wound  type,  and  in  alternating  currents,  the  Slip 
Ri-ng  type  of  motor. 

The  types  of  controls  to  use  for  the  motors  are  fully  given  in 
Section  4. 

Data  Required    for  Estimates  for    Power  Pumps 
and  Crank  and  Fly  Wheel  Pumps. 

1.  For  what  purpose  is  pump  to  be  used? 

2.  (a)  Capacity  of  pump  in  U.  S.  gallons  per  minute. 

(b)  If  the  pump  is  for  vacuum  service,  give  the  number  of 
square  feet  of  radiation,  or  the  number  of  cubic  foot  displace- 
ment per  minute  required. 

(c)  If  pump  is  for  use  with  a  condenser,  give  the  number  of 
pounds  of  steam  to  be  condensed  per  hour,  the  temperature 
of  condensing  water,  the  vacuum  to  be  carried  and  the  type 
of  condenser. 

(d)  If  pump  is  for  evaporator  service  give  the  nature  of  the 
liquor  to  be  evaporated,  the  quantity  of  liquor  to  be  evapo- 
rated per  hour,   the  temperature   of  condensing  water,   the 
vacuum  under  which  the  liquid  is  to  be  evaporated,  and  the 
number  of  effects  in  the  evaporator? 

3.  Total  lift,  including  suction  discharge  lift,  and  pipe  friction 
in  feet. 

4.  Length  and  diameter  of  suction  pipe  ? 

5.  Vertical  distance  from  water  level  to  pump  in  feet? 

6.  Number  and  size  of  elbows  in  suction  pipe  ? 

7.  Length  and  diameter  of  discharge  pipe  ? 

8.  Vertical  distance  above  pump,  or  against  what  pressure  is 
liquid  to  be  discharged  ? 

9.  Number  and  size  of' elbows  in  discharge  pipe? 

10.  Number  and  diameter  of  valves  in  discharge  pipe? 

11.  Temperature  of  liquid  in  degrees  Fah.  ? 

12.  Specific  gravity  of  liquid? 

13.  Nature  of  liquid  to  be  handled:    Fresh  water,  salt  water, 
acidulous,  alkaline,  gritty,  etc.  ? 

14.  If  pump  is  to  be  motor  driven,  state  characteristics  of  cur- 
rent?   If  direct  current,  give  voltage,  if  alternating  current 

give  voltage,  cycles,  and  phase  ? 

15.  If  pump  is  to  be  belt  driven  give  the  dimensions  and  speed 
of  the  driving  pulley  ? 

16.  If  pump  is  t6  be  of  the  crank  and  flywheel  type,  give  the 
lowest  steam  pressure  to  be  used  at  the  pump? 

17.  (a)  Will  pump  exhaust  into  the  atmosphere? 

(b)  Will  pump  exhaust  into  a  heater  (State  whether  open  or 
closed). 

18.  What  pressure  will  pump  exhaust  against  ? 

19.  If  pump  is  to  operate  condensing  give  vacuum  to  be  carried 
on  the  condenser. 

20.  Where  is  pump  to  be  located  ? 


L 


386 


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lie 

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S. 

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Fig.  158 

Single  Belt  Driven 
Piston  Pump. 


Fig.  163 

Electric  Gear  Driven 
Piston   Pump 


Single  Piston  Pattern  Pressure  Pumps 

150  Pounds  Maximum  Pressure 


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5 

6.60 

40 

264 

15840 

42x8 

5 

10    x!2 

8 

6 

8.15 

40 

326  i    19560 

42x8 

5 

|       AND 

CONDEN 

SERS 

FOR 

EVERY 

S 

ERVICE      ™| 

387 


STEAM       PUMP       COMPANY 


Fig.  165 
Belt  Driven  Pump 


Fig.  166 
Motor  Driven  Pump 


Single  Piston  Pattern  Light  Service  Pumps 

75  Pounds  Maximum  Pressure 


o 

|'s» 

c 

i 

N 

ll| 

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3  V£ 

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99 

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117 

7020 

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12540 

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469 

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640 

38400 

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16    x!2 

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10 

8 

20.88 

40 

835 

50100 

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5 

388 


Fig.  167 
Belt  Driven  Pump 


Fig.  168 
Motor  Driven  Pump 


Standard  Pattern  Wet  Vacuum  Pumps 

Maximum  Vacuum  26 "  with  30 "  Barometer 


CAPACITY 

c. 

1 

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w 
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15 

20    x20 

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20 

I 


UNION       STEAM       PUMP       COMPANY 


Fig.  93 


Single  Belt-Driven  Dry- Vacuum  Pumps 

28>i"-29"  Vacuum,  30 "  Barometer 


Air 
Cylinder 

1 

Displacement 
Cubic  Feet 
Free  Air 

ll 

Pipe  Openings 

Driving 
Pulley 

a 

S 
1 

1 

"s 

| 

G 

11 

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& 

rt 

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150 

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3 

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y* 

28 

6 

28 

14 

6 

275 

1.06  , 

292 

12 

4 

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y?, 

28 

6 

28 

18 

6 

275 

1.70 

483 

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5 

5 

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28 

6 

28 

18 

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22 

5 

5 

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8 

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8 

250 

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880 

31 

7 

6 

42 

8 

42 

22 

10 

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37 

7 

6 

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48 

10 

48 

26 

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8 

7 

48 

10 

48 

28 

12 

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8.56 

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65 

9 

8 

y*. 

66 

12 

55 

30 

12 

220 

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2160 

75 

10 

8 

1^3 

66 

12 

55 

32 

15 

210 

13.98 

2940 

100 

12 

10 

y* 

72 

15 

60 

PUMPING    MACHINERY,    AIR   COMPRESSORS 


390 


B- 

BATTLE 

C  REEK. 

MICHIGAN, 

U.  S.  AfT 

Fig.  170 


Power  Magma  Pumps 

75  Pounds  Maximum  Pressure 


Size  of 

Size  of 

Displacement 

Pump 

Openings 

of  Piston 

&  «•« 

'ft      S'w 

a 

A 

B 

£ 

g 

•D 
I 

o^fc'o  3'^ 

3 

X 

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ll 

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c  Si 

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8 

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6 

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*The  actual  amount  of  liquor  handled  with  a  magma  pump  is  60%  of  its  piston 
displacement. 


AND    CONDENSERS    FOR    EVERV  SERVICE      _f 

nBmvn»»vatt  w  vv  mrg-g-gTrir_c£j^am'tf  t  yTi^^  T^  ff^tt  a-a"jr^fl^JJrrTra^r-ir»r-jftra  aTw'a  w"w»r»^~v»ir»  w«»n»»»»  g=w=rf» 


391 


STEAM       PUMP       COMPANY 


Fig.  207. 


Single  Power  Pumps 

Self-Oiling  Type 

231  Feet  Maximum  Pressure. 


3 

SIZE  OF 
PUMP 

ft 

c/)  Q) 

C  +J 

H, 
a 

§£•£ 
^. 

1 

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w 

s  a 

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£ 

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870 

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50 

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1620 

3 

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50 

42.5 

2550 

4K 

16  x  4 

2H 

2^ 

6x6 

50 

73. 

4380 

8.0 

24  x  4 

3 

3 

392 


REEK 


MICHIGAN 


U.  S.  A. 


Fig.  206. 
Belt-Driven  Pump. 


Duplex  Power  Pumps 

Self-Oiling  Type 


Size 

3 

3 

Capacity                    Pipe 

r\  :  

Pulleys 

•§§ 

.2 

Belt 

I 

||  . 

J 

<u 

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i 

II 

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f-l   .-H 

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75 

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16 

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150 

75 

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4 

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75 

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60 

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6 

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60 

2.69 

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6 

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85 

60 

2.93 

175 

4 

3 

24 

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10 

300 

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4 

3 

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8 

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10 

250 

50 

3.74 

187 

4 

3 

36 

8 

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6 

10 

200 

50 

4.89 

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5 

4 

36 

8 

D 

7 

10 

150 

50 

6.66 

333 

6 

5 

36 

8 

D 

10 

100 

50 

9.80 

490 

6 

5 

36 

8 

D 

io2 

10 

75 

50 

13.6 

680 

8 

6 

36 

8 

D 

393 


Fig.  208. 


Union  Duplex  Power  Pumps 
Oil  Line  Pumps 

Self-Oiling  Type 


Size 

g 

Capacity 

Openings 

Pulleys 

.2 

.ripe 

«J 

ojj 

& 

J 

2 
S 

Maximum  Oi 
Pressure 

Max.  Revolut 
of  Crankshaft 
per  Minute 

Gals,  per 
,  Revolution 

M 

II 

Barrels  per 
Hour 
(42  Gallons 
per  Barrel) 

Suction 

Discharge 

Diameter 

.2 

"a 

& 

c 

^ 
Jj 

in 

*. 

^3 

II 

3 

6 

350 

60 

.74 

44 

63 

21A 

2 

24 

5 

D 

3^ 

6 

250 

60 

.99 

59 

84 

VA 

2 

24 

5 

D 

3 

8 

450 

55 

.98 

54 

77 

VA 

2 

28 

6 

D 

3>i 

8 

350 

55 

1.33 

73 

104 

21A 

2 

28 

6 

D 

^ 

3 

10 

800 

50 

1.22 

61 

87 

3 

2 

36 

8 

D 

tr 

3^ 

10 

800 

50 

1.67 

84 

120 

3 

2 

36 

8 

D 

4 

10 

450 

50 

2.17 

108 

154 

4 

3 

36 

8 

D 

4^ 

10 

350 

50 

2.75 

137 

196 

4 

3 

36 

8 

D 

393A 


BATTLE      CREEK.     MICHIGAN,      U.  S.  A. 


1 


Fig.  185 

Union  Duplex  Power  Cargo 
Oil  Pumps 


Sbe  of  Pump 

L  iameter  of 

RATINGS 

P          n  Onpnincrc 

w 

3 

.rump  vjpemngb 

ri 

0) 

o 
£ 

«. 

M 

I 

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rt^ 

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a 

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a 

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10 

12 

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125 

40 

16.3 

652 

931 

10H 

12 

10 

8 

110 

40 

17.8 

712 

1020 

11 

12 

10 

8 

100 

40 

19.7 

788 

1120 

12 

15 

14 

12 

125 

40 

29.4 

1176 

1670 

13 

15 

14 

12 

100 

40 

34.5 

1380 

1970 

14 

15 

14 

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90 

40 

40.0 

1600 

2280 

393B 


UNION 


» J- _«  « .*  _«A1.1A*A**J 

S  TEAM 


PUMP       COM  PANY 


Fig.  173 


Duplex  Belt  Driven  Enclosed  Type  Dry 
Vacuum  Pumps 

28%  "-29"  Vacuum  30 "  Barometer 


Air 
Cylinders 

Displacement 
C;ibic  Feet 
Free  Air 

1 

Pipe  Openings 

Driving 
Pulley 

I      <u 

J3 

| 

c 

h 

*lf 

1 

g 

w 

^ 

c 

jj 

<? 

<o 

Diameter 

| 

£ 
£ 

"y  V 

II 

ll 

ill 

SuctionF 

50 
C 

1 

Q 

MM 

C.      l-H 

Diamete; 

"o 

J3 

II 

18 

8 

250 

4.70 

1180 

44 

5 

5 

M 

54 

10 

22 

8 

250 

7.04 

1760 

62 

7 

6 

M 

54 

10 

22 

10 

235 

8.80 

2070 

74 

7 

6 

54 

It 

26 

10 

235 

12.30 

2890 

98 

8 

7 

1 

54 

14 

28 

12 

220 

17.12 

3760 

130 

9 

8 

1 

66 

18 

30 

12 

220 

19.64 

4320 

150 

10 

8 

l 

66 

18 

32 

15 

210 

27.96 

5880 

200 

12 

10 

i 

80 

25 

394 


Fig.  160 


Triplex  Belt  Driven  Plunger  Pumps 

2000  Pounds  Maximum   Pressure 


Size  of 

. 

>>   »H 

Openings 

SIZE 

I* 

1H 

| 

i 

Size  of 
Pulley 

O*   " 

ol  *rt  '** 

o 

M  rt 

GO^ 

a 

in 

iS-S 

1       x  3 

150 

4K 

1 

K 

24  x  5 

1M  x  4 

150    . 

9K 

IK 

1 

48  x  6 

IK  x  4 

150 

13K 

IK 

1 

48  x  6 

395 


Fig.  174 


Triplex  High  Pressure  Milk  Pumps 

A  special  type  of  Triplex  Power  Pump  for  Spraying  or  Atomizing  Con- 
densed Milk  in  the  manufacture  of  Dry  or  Powdered  Milk. 


Table  of  Capacities,  Pressures*  etc. 


Size 

2J 

OH* 

u 

& 

E 

fc 

o 

05 

w  3 

0*0 

la 

11 

0 

£ 

CO 

X 

II 

II 

II 

i 

1 

3 

100 

.275 

1650 

3000 

16  x  3 

1 

4 

100 

.367 

2200 

3500 

20  x  5 

4 

100 

.572 

3430 

3000 

20  x  5 

1^2 

4 

100 

.820 

4920 

2000 

20  x  5 

1M 

4 

60 

1.10 

4607 

900 

20  x  5 

2 

4 

60 

1.47 

5286 

900 

20  x  5 

NOTE.  —  Capacities  are  based  on  milk  weighing  nine  pounds  per  gallon 
after  condensing  5  to  1. 

Suction  opening  on  3-inch  stroke  pumps,  1%-inch  standard  pipe  tap. 
l2<2-mch  sanitary  union. 


Discharge  opening  on  3-inch  stroke  pumps,  J^-inch  standard  pipe  tap. 
.Suction  opening  on  4-inch  stroke  pumps,  1^-inch  standard  pipe  tap. 
Discharge  opening  on  4-inch  stroke  pumps,  1-inch  standard  pipe  tap. 


%T~    PV^PlWG    T^ACHINiERY,    AIR 

COMPRESSORS 

J 

396 


Fig.  209. 

The  Viscolizer 

The  Viscolizer  is  a  specially  designed,  powerfully  constructed  triplex  pump 
used  in  the  manufacture  and  processing  of  liquid  and  semi-liquid  foods,  med- 
icine, drugs  and  oil  emulsions.  The  possibility  of  storing  and  marketing 
evaporated  milk  is  due  entirely  to  the  ability  of  this  machine  to  prevent 
separation  of  the  butter  fat  from  the  milk. 

In  salad  dressings  and  medicines  or  other  oil  emulsions  of  similar  character 
the  oil  is  so  thoroughly  mixed  with  the  water  by  being  forced  under  high 
pressures  through  the  specially  constructed  emulsifying  device  that  it  will 
not  separate  and  can  therefore  be  marketed  to  advantage. 

The  process  is  relatively  new  and  requires  primarily  a  sturdy  pump 
which  will  maintain  even  pressures  in  the  emulsifying  device.  These  re- 
quisites are  best  met  by  the  triplex  design  and  especially  by  that  shown  in 
figure  209. 


Sizes,  Capacities  and  Installation  Data 


i-i 

VI    3 

. 

bo 

-c 

>, 

>, 

e.2 

oX 

<u  •£ 

i2j 

H.2 

'c'S 

£cw 

li 

^«'3 

&.* 

sJIsr 

1 

"a  fe 
OP 

SI 

foil 

Ow 

aw 

%* 

ElJf 

-2  GO, 
^^S 

5li 

100 

100 

12x2  ^ 

480 

4tol 

120 

3 

900 

30x36 

1 

i 

200 

200 

16x3 

500 

5tol 

100 

1500 

30x48 

l/^ 

i/^ 

300 

300 

20x5 

500  to  600 

6  to  1 

100 

10  ° 

2300 

48x60 

1^ 

i/^ 

450 

450 

20x5 

500  to  600 

6  to  1 

90  to  100 

15 

2500 

50x66 

\l/2 

\^/ft 

800 

800 

28x6 

450 

5  to  1 

90 

25 

4000 

56x78 

2 

11A 

397 


STEAM       PUMP       COMPANY 


Fig.  176 


Single  Crank  and  Flywheel  Wet  Vacuum  Pumps 

28 "  Vacuum,  with  30"  Barometer 


Size  of  Pump 

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28"  Vacuum,  with  30 "  Barometer 


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MV 


Appendix 


T\ 


jj        UNION 

STEAM 

P  UM  P 

C  6  M  P  ANY      ™! 

Creating  a  Vacuum  in  a  Closed  Tank 

Quite  often  it  is  necessary  to  calculate  the  size  of  vacuum  pump  to  exhaust 
a  vessel  of  known  capacity  in  a  stated  time  to  a  certain  degree  of  vacuum,  and 
for  this  purpose  the  following  table  has  been  calculated.  It  gives  the  volume 
which  must  be  exhausted  from  vessels  in  order  to  reduce  the  pressure  from  one 
atmosphere  P  to  the  lower  pressure  Pi .  If  the  time  is  given  in  which  a  desired 
effect  is  to  be  produced,  the  size  of  pump  can  be  readily  calculated. 

Table  giving  the  number  of  cubic  feet  that  must  be  exhausted  from  a  closed 
vessel  containing  100  to  4500  cubic  feet  in  order  to  reduce  the  original  internal 
pressure  from  (14.7  Ibs.)  to  .9  -  .01  atmospheres  absolute  or  3"  -  29  3-4"  vacuum. 


If  the  original  pressure  in  a  vessel  is  atmosphere  absolute  or  P 
and  it  is  to  be  reduced  to  Pi    the  following  volumes  of  air  must 


The  pressure  in 
the  vessel  is  to 

be  exhausted 

be  reduced  from 

atmosphere  - 
to  -  Pi 

P 

Capacity  of  the  vessel  in  cubic  feet 

100 

500 

1000 

1500 

2000 

2500 

3000 

3500 

4000 

4500 

Atmos. 

Vac. 

Abs. 

Inch. 

Cubic  feet  to  be  exhausted 

.9 

.8 

3 

6 

10.5 
22.5 

53 
113 

105 

225 

158 
338 

210 
450 

263 
563 

315 

675 

368 

788 

424 
900 

473 
1013 

.7 

9 

35 

175 

350 

525 

700 

875 

1050 

1225 

1400 

1575 

.6 

12 

51 

255 

510 

765 

1020 

1275 

1530 

17S5 

2040 

2295 

.5 

15 

69 

345 

690 

1035 

1380 

1725 

2070 

2415 

2760 

3106 

.4 

-18 

91.5 

458 

915 

1374 

1830 

'  2290 

2745 

3203 

3660 

4118 

.3 

21 

120 

600 

1200 

1800 

2400 

3000 

3600 

4200 

4800 

5400 

.25 

22J4 

138 

600 

1380 

2070 

2760 

3450 

4140 

4S30 

5520 

6210 

.2 

24 

161 

805 

1610 

2415 

3220 

4025 

4830 

5635 

6440 

7245 

.15 

25YZ 

190 

950 

1900 

2850 

3800 

4750 

5700 

6650 

7600 

8550 

.1 

27 

230 

1150 

2300 

3150 

4600 

5750 

6900 

8050 

9200 

10350 

.09 

27]4 

241 

1205 

2410 

3615 

4820 

6025 

7230 

8435 

9640 

10845 

.08 

27  1A 

252 

1260 

2520 

3780 

5010 

6300 

7560 

8820 

10080 

11340 

.07 

27H 

266 

1330 

2660 

3990 

5320 

6650 

7980 

9310 

10640 

11970 

.06 

28X, 

281 

1405 

2810 

4215 

5620 

7025 

8430 

9835 

11240 

12645 

.05 

28M 

300 

1500 

3000 

4500 

6000 

7500 

9000 

10500 

12000 

13500 

.04 

28% 

322 

1610 

3220 

4830 

6440 

8050 

9660 

11270 

12880 

14490 

.03 

29 

351 

1755 

3510 

5265 

7020 

8775 

10530 

12285 

14040 

15795 

.02 

29^ 

391 

1955 

3910 

5865 

7820 

9775 

11730 

13685 

15640 

17595 

.01 

29H 

460 

2300 

4600 

6900 

9200 

11500 

13800 

16100 

18100 

20700 

EXAMPLE. 

We  have  a  closed  tank  of  500  cubic  feet  capacity  at  atmospheric  pressure, 
and  it  is  desired  to  exhaust  it  down  to  21"  of  vacuum  in  five  minutes  time. 
What  capacity  in  cubic  feet  per  minute  must  the  air  pump  have? 

SOLUTION. 

Referring  to  the  table  opposite  21"  of  vacuum,  it  is  seen  for  a  vessel  of 
500  cubic  feet  capacity,  600  cubic  feet  must  be  exhausted.  If  this  amount 
must  be  exhausted  in  five  minutes  time,  the  capacity  of  the  air  pump  must 
be  one-fifth  of  600  or  120  cubic  feet  per  minute. 


404 


|        BATTLE 

C 

RE 

EK. 

'  M 

1C 

H 

IGAN. 

U. 

s 

-C^J 

Creating  a  Vacuum  in  a  Closed  Tank — Continued 

If  it  is  required  to  reduce  the  pressure  in  a  vessel  from  ?2,  which  is  lower 
than  the  atmosphere  to  the  still  lower  pressure  Pi,  in  order  to  calculate  the 
volume  of  air  to  be  exhausted,  in  this  case,  it  is  necessary  to  subtract  the 
volume  which  must  be  exhausted  in  order  to  reduce  the  pressure  from  atmos- 
phere to  Pa,  from  that  required  to  reduce  the  pressure  from  atmosphere  to  Pi. 

EXAMPLE. 

The  vacuum  in  a  closed  tank  of  2000  cubic  feet  capacity  is  15",  and  this 
is  to  be  reduced  to  27"  of  vacuum.  What  volume  must  be  exhausted? 

SOLUTION. 

From  the  table  it  is  seen  4600  cubic  feet  must  be  exhausted  to  lower  the 
pressure  from  atmosphere  to  27"  of  vacuum.  Also  it  will  be  seen  from  the 
table  1380  cubic  feet  must  be  exhausted  to  lower  the  pressure  from  atmosphere 
to  15"  of  vacuum.  The  difference  between  these  two  values  equals  3220 
cubic  feet  that  must  be  exhausted  to  lower  the  pressure  from  1,5"  of  vacuum 
to  27"  of  vacuum. 

Having  calculated  the  capacity  required  for  the  vacuum  pump,  the 
displacement  of  the  vacuum  pump  must  next  be  determined.  This  is  cal- 
culated by  assuming  the^ volumetric  efficiency  of  the  vacuum  pump  as  60-75%. 
Then  the  displacement  in  cubic  feet  per  minute  equals  the  capacity  in  cubic 
feet  per  minute  divided  by  the  volumetric  efficiency  expressed  as  a  decimal. 


AND   CONDENSERS    FOR   EVERV  SERVTCET 


405 


BUNION 

ST 

EA 

M 

P 

U 

M 

P 

C 

0  M 

PANY 

a 

Properties  of  Saturated  Steam 

(Condensed  from  Marks  and  Davis's  Steam  Tables  and  Diagrams,  1909,  by  per- 
mission of  the  publishers,  Longmans,  Green  &  Co.) 


Total  Heat 

jT 

above  30°  F. 

S 

. 

tn 

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M  G 

to 

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£l, 

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of  Merc 

l! 

Tempera' 
Fahrenr. 

In  the  WTa 
h 
Heat-Uni 

a  g 

fi 

1«| 

Volume, 
in  1  Lb. 

21 

.COT 
M 

[>fi| 

Entropy 
Water. 

Entropy 
oration. 

29.74 

0.0886 

32 

0.00 

1073.4 

1073.4 

3294 

0.000304 

0.0000 

2.1832 

29.67 

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40 

8.05 

1076.9 

1068  .  9 

2438 

0.000410 

0.0162 

2.1394 

29.56 

0.1780 

50 

18.08 

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0.000587 

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2.0865 

29.40 

0.2562 

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0.000828 

0.0555 

2.0358 

29.18 

0  .  3626 

70 

38.06 

1090.3 

1052.3 

871 

0.001148 

0.0745 

1.9868 

29.89 

0.505 

80 

48.03 

1094.8 

1046  .  7 

636.8 

0.001570 

0.0932 

1.9398 

28.50 

0.696 

90 

58.00 

1099  .  2 

1041.2 

469.3 

0.002131 

0.1114 

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28.00 

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100 

67.97 

1103.6 

1035.6 

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0.1295 

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101.83 

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1034.6 

333.0 

0.00300 

0.1327 

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126.15 

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0.00576 

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23.81 

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141.52 

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118.5 

0.00845 

0  .  2008 

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21.78 

4 

153.01 

120.9 

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19.74 

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162.28 

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1.6084 

17.70 

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170.06 

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61.89 

0.01616 

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176.85 

144.7 

1136.5 

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1  .  5582 

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8 

182.86 

150.8 

1139.0 

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47.27 

0.02115 

0.2673 

1  .  5380 

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188.27 

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985.0 

42.36 

0.02361 

0  .  2756 

1  .  5202 

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193.22 

161.1 

1143.1 

9-82.0 

38.38 

0.02606 

0.2832 

1  .  5042 

7.52 

11 

197.75 

165.7 

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979.2 

35.10 

0.02849 

0  .  2902 

1.4895 

5.49 

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201.96 

169.9 

1146.5 

976.6 

32.36 

0.03090 

0.2967 

1.4760 

3.45 

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205.87 

173.8 

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1.4639 

1.42 

14 

209  .  55 

177.5 

1149.4 

971.9 

28.02 

0.03569 

0.3081 

1.4523 

Ibs. 

gage 

14.70 

212 

180.0 

1150.4 

970.4 

26.79 

0.03732 

0.3118 

1.4447 

03 

15 

213.0 

181.0 

1150.7 

969.7 

26.27 

0.03806 

0.3133 

1.4416 

1.3 

16 

216.3 

184.4 

1152.0 

967.6 

24.79 

0.04042 

0.3183 

1.4311 

2.3 

17 

219.4 

187.5 

1153.1 

965.6 

23.38 

0.04277 

0.3229 

1.4215 

3.3 

18 

222.4 

190.5 

1154.2 

963.7 

22.16 

0.  '04512 

0  .  3273 

1.4127 

4.3 

19 

225.2 

193.4 

1155.2 

961.8 

21.07 

0.04746 

0.3315 

1.4045 

5.3 

20 

228.0 

196.1 

1156.2 

960.0 

20.08 

0.04980 

0.3355 

1.3965 

6.3 

21 

230.6 

198.8 

1157.1 

958.3 

19.18 

0.05213 

0.3393 

1.3887 

7.3 

22 

233.1 

201.3 

1158.0 

956.7 

18.37 

0.05445 

0.3430 

1.3811 

8.3 

23 

235.5 

203.8 

1158.8 

955.1 

17.62 

0.05676 

0.3465 

1.3739 

9.3 

24 

237.8 

206.1 

1159.6 

953.5 

16.93 

0.05907 

0.3499 

1.3670 

10.3 

25 

240.1 

208.4 

1160.4 

952.0 

16.30 

0.0614 

0.3532 

1  .  3604 

11.3 

26 

242.2 

210.6 

1161.2 

950.6 

15.72 

0.0636 

0.3564 

1.3542 

12.3 

27 

244.4 

212.7 

1161.9 

949.2 

15.18 

0.0659 

0  .  3594 

1.3483 

13.3 

28 

246.4 

214.8 

1162.6 

947.8 

14.67 

0.0682 

0.3623 

1.3425 

14.3 

29 

248.4 

216.8 

1163.2 

946.4 

14.19 

0.0705 

0.3652 

1.3367 

15.3 

30 

250.3 

218.8 

1163.9 

945.1 

13.74 

0  .  0728 

0  .  3680 

1.3311 

16.3 

31 

252.2 

220.7 

1164.5 

943.8 

13.32 

0.0751 

0.3707 

1.3257 

17.3 

32 

254.1 

222.6 

1165.1 

942.5 

12.93 

0.0773 

0.3733 

1.3205 

18.3 

33 

255.8 

224.4 

1165.7 

941.3 

12.57 

0.0795 

0.3759 

1.3155 

19.3 

34 

257.6 

226.2 

1166.3 

940.1 

12.22 

0.0818 

0  .  3784 

1.3107 

20.3 

35 

259.3 

227.9 

1166.8 

938.9 

11.89 

0.0841 

0.3808 

1.3060 

21.3 

36 

261.0 

229.6 

1167.3 

937.7 

11.58 

0.0863 

0.3832 

1.3014 

22.3 

37 

262.6 

231.3 

1167.8 

936.6 

11.29 

0.0886 

0.3855 

1.2969 

23.3 

38 

264.2 

232.9 

1168.4 

935.5 

11.01 

0.0908 

0.3877 

1.2925 

24.3 

39 

265.8 

234.5 

1168.9 

934.4 

10.74 

0.0931 

0.3899 

1  .  2882 

25.3 

40 

267.3 

236.1 

1169.4 

933.3 

10.49 

0.0953 

0.3920 

1.2841 

26.3 

41 

268.7 

237.6 

1169.8 

932.2 

10.25 

0.0976 

0.3941 

1.2800 

J^ 


406 


1- 

BATTLE 

CREEK.     MICHIGAN, 

J^A,:;;f 

Properties  of  Saturated  Steam — Continued 


'  Total  Heat 

i« 

above  32°  F. 

, 

m  g 

.  . 

& 

ijj  t.H 

w1-1 

cti 

PT    <L* 

r^  *~ 

4) 

9 

y 

8+J 

I  t! 

I  i 

IB 

.W 

G*o 

*"*  s 

A 

•a 

w 

*o 

«& 

s 

11 

$  '1 

!J 

*&i 

jjS 

££ 

ii 

>.  d 
M 

^.a 

g  jn 

•§"*! 

.H1""1 

'tf*J 

£  a 

51 

0J 

^ 

gfc 

S  « 

a  « 
i—  i 

*°.S 

f 

& 

£° 

27.3 
28.3 

42 

43 

270.2 

271.7 

239.1 
240  .  5 

1170.3 
1170.7 

931.2 
930.2 

10.02 
9.80 

0.0998 
0.1020 

0.3962 
0.3982 

1.2759 
.2720 

29.3 

44 

273.1 

242.0 

1171.2 

929.2 

9.59 

0.1043 

0.4002 

.2681 

30  .  3 

45 

274.5 

243.4 

1171.6 

928.2 

9.39 

0.1065 

0.4021 

.2844 

31  3 

46 

275.8 

244.8 

1172.0 

927.2 

9.20 

0.1087 

0.4040 

.2607 

32.3 

47 

277.2 

246.1 

1172.4 

926.3 

9.02 

0.1109 

0.4059 

.2571 

33.3 

48 

278.5 

247.5 

1172.8 

925.3 

8.84 

0.1131 

0.4077 

.2536 

34.3 

49 

279.8 

248.8 

1173.2 

924.4 

8.67 

0.1153 

0.4095 

.2502 

35.3 

50 

281.0 

250.1 

1173.6 

923.5 

8.51 

0.1175 

0.4113 

.2468 

38.3 

51 

282.3 

251.4 

1174.0 

922.6 

8.35 

0.1197 

0.4130 

.2432 

37.3 

52 

283.5 

252.6 

1174.3 

921.7 

8.20 

0.1219 

0.4147 

.2405 

38.3 

53 

284.7 

253.9 

1174.7 

920.8 

8.05 

0.1241 

0.4161 

.  2370 

39.3 

54 

285.9 

255.1 

1175.0 

919.9 

7.91 

0.1263 

0.4180 

.2339 

40.3 

55 

287.1 

256.3 

1175.4 

919.0 

7.78 

0.1285 

0.1496 

.  2309 

41.3 

56 

288.2 

257.5 

1175.7 

918.2 

7.  05 

0.1307 

0.4212 

.2278 

42.3 

57 

289.4 

258.7 

1176.0 

917.4 

7.52 

0.1329 

0.4227 

.2248 

43.3 

58 

290.5 

259.8 

1176.4 

916.5 

7.40 

0.1350 

0.4242 

.2218 

44.3 

59 

291.6 

261.0 

1176.7 

915.7 

7.28 

0.1372 

0  .  4257 

.2189 

45.3 

60 

292.7 

262.1 

1177.0 

914.9 

7.17 

0.1394 

0.4272 

.2160 

46.3 

61 

293.8 

263.2 

1177.3 

914.1 

7.06 

0.1416 

0.4287 

.2132 

47.3 

62 

294.9 

264.3 

1177.6 

913.3 

6.95 

0.1438 

0.4302 

.2104 

48.3 

63 

295.9 

265.4 

1177.9 

912.5 

6.85 

0  .  1460 

0.4316 

.2077 

49.3 

64 

297.0 

266.4 

1178.2 

911.8 

6.75 

0.1482 

0.4330 

.2050 

50.3 

65 

298.0 

267.5 

1178.5 

911.0 

6.65 

0.1503 

0.4344 

.2024 

51.3 

66 

299.0 

268.5 

1178.8 

910.2 

6.56 

0.1525 

0.4358 

.1998 

52.3 

67 

300.0 

269.6 

1179.0 

909.5 

6.47 

0.1547 

0.4371 

.1972 

53.3 

68 

301.0 

270.6 

1179.3 

908.7 

6.38 

0.1569 

0.4385 

.1946 

54.3 

69 

302.0 

271.6 

1179.6 

008.0 

6.29 

0.1590 

0.4398 

.1921 

55.3 

70 

302.9 

272.6 

1179.8 

907.2 

6.20 

0.1621 

0.4411 

.1896 

56.3 

71 

303.9 

273.6 

1180.1 

906.5 

6.12 

0.1634 

0.4424 

.1872 

57.3 

72 

304.8 

274.5 

1180.4 

905.8 

6.04 

0.1656 

0.4437 

.1848 

58.3 

73 

305.8 

275.5 

1180.6 

905.1 

5.96 

0.1678 

0.4449 

.1825 

59.3 

74 

306  .  7 

276.5 

1180.9 

904.4 

5.89 

0.1699 

0.4462 

.1801 

60.3 

75 

307.6 

277.4 

1181.1 

903.7 

5.81 

0.1721 

0.4474 

.1778 

61.3 

76 

308.5 

278.3 

1181.4 

903.0 

5.74 

0.1743 

0.4487 

.  1755 

62.3 

77 

309.4 

279.3 

1181.6 

902.3 

5.67 

0.1764 

0.4499 

.1730 

63.3 

78 

310.3 

280.2 

1181.8 

901.7 

5.60 

0.1786 

0.4511 

.1712 

64.3 

79 

311.2 

281.1 

1182.1 

901.0 

5.54 

0.1808 

0.4523 

.1687 

65.3 

80 

312.0 

282.0 

1182.3 

900.3 

5.47 

0.1829 

0.4535 

.1665 

66.3 

81 

312.9 

282.9 

1182.5 

899.7 

5.41 

0.1851 

0.4546 

.1644 

67.3 

82 

313.8 

283.8 

1182.8 

899.0 

5.34 

0.1873 

0.4557 

.1623 

68.3 

83 

314.6 

284.6 

1183.0 

898.4 

5.28 

0.1894 

0.4568 

.1602 

69.3 

84 

315.4 

285.5 

1183.2 

897.7 

5.22 

0.1915 

0.4579 

.1581 

70.3 

85 

316.3 

286.3 

1183.4 

897.1 

5.16 

0.1937 

0.4590 

.1561 

71.3 

86 

317.1 

287.2 

1183.6 

896.4 

5.10 

0.1959 

0.4601 

.1540 

72.3 

87 

317.9 

288.0 

1183.8 

895.8 

5.05 

0.1980 

0.4612 

.1520 

73.3 

88 

318.7 

288.9 

1184.0 

895.2 

5.00 

0.2001 

0.4623 

.1500 

74.3 

89 

319.5 

289.7 

1184.2 

894.6 

4.94 

0.2023 

0.4633 

.1481 

75.3 

90 

320.3 

290.5 

1184.4 

893.9 

4.89 

0  .  2044 

0.4644 

.1461 

76.3 

91 

321.1 

291.3 

1184.6 

893.3 

4.84 

0  .  2065 

0.4654 

.1442 

77.3 

92 

321.8 

292.1 

1184.8 

892.7 

4.79 

0  .  2087 

0.4664 

.1423 

78.3 

93 

322.6 

292.9 

1185.0 

892.1 

4.74 

0.2109 

0.4674 

.1404 

79.3 

94 

323.4 

293.7 

1185.2 

891.5 

4.69 

0.2130 

0.4684 

.1385 

80.3 

95 

324.1 

294.5 

1185.4 

890.9 

4.65 

0.2151 

0.4694 

.1367 

AND    CONDENSERS    FOR   EVERY"  SERVICE 


a 

N 

I  0 

N 

STE 

AM 

P 

U 

M 

P 

C  O 

MPANY 

Properties  of  Saturated  Steam — Continued 


Total  Heat 

V 

ft 

above  32°  F. 

•  1 

i 

*  • 

Z  c 

•>  ^ 

**  H 

a 

1? 

fl 

u 

j| 

u 

4)    c/1 

S  |J 

a 
-*-"  ^ 

«•* 

0*0 

^H 

4) 

£ 

"o 

W 

<u  ^ 

3  ^ 

cu  § 

£  £ 

^J^+J 

•*•>  '   M 

c"5 

SM 

ft  £ 

0,0 

00  w 

P-^q 

V    +- 

Js  "* 

gffi.tj 

3  J~t 

.£? 

s  ** 

8*^ 

^5 

J3  "j 

If? 

->->  5 

*"  W 

"a  II  |D 

"o_c 

t>£ 

s£ 

"c  ^ 

0 

< 

£  W 

c 

' 

w 

W 

81.3 
82.3 

96 
97 

324.9 
325.6 

295.3 
296.1 

1185.6 
1185.8 

890.3 

889.7 

4.60 
4.56 

0.2172 
0.2193 

0.4704 
0.4714 

1  .  1348 
1.1330 

83.3 

98 

326.4 

296.8 

1186.0 

889.2 

4.51 

0.2215 

0.4724 

1.1312 

84.3 

99 

327.1 

297.6 

1186.2 

888.6 

4.47 

0.2237 

0.4733 

1.1295 

85.3 

100 

327.8 

298.3 

1186.3 

888.0 

4.429 

0.2258 

0.4743 

1.1277 

8V.  3 

102 

329.3 

299  .  8 

1186.7 

886.9 

4.347 

0.2300 

0.4762 

1.1242 

89.3 

104 

330.7 

301.3 

1187.0 

885.8 

4.268 

0  .  2343 

0.4780 

1.1208 

91.3 

106 

332.0 

302.7 

1187.4 

884.7 

4.192 

0.2336 

0.4798 

1.1174 

93.3 

108 

333.4 

304.1 

1187.7 

883.6 

4.118 

0  .  2429 

0.4816 

1.1141 

95.3 

110 

334.8 

305.5 

1188.0 

882.5 

4.047 

0  .  2472 

0.4834 

1.1108 

97.3 

112 

336.1 

306.9 

1188.  4 

881.4 

3.978 

0.2514 

0.4852 

1  .  1076 

99.3 

114 

337.4 

308.3 

1188.7 

880.  4 

3.912 

0.2556 

0  .  4869 

1  .  1015 

101.3 

116 

338.7 

309.6 

1189.0 

879.3 

3  .  848 

0.2599 

0.4886 

1.1014 

103.3 

118 

340.0 

311.0 

1189.3 

878.3 

3.786 

0.2641 

0.4903 

1  .  008  1 

105.3 

120 

341.3 

312.3 

1189.6 

877.2 

3.726 

0.2683 

0.4919 

1.0951 

107.3 

122 

342.5 

313.6 

1189.8 

876.2 

3.668 

0.2726 

0.4935 

1.0924 

109.3 

124 

343.8 

314.9 

1190.1 

875.2 

3.611 

0.2769 

0.4951 

1.0895 

111.3 

126 

345.0 

316.2 

1190.4 

874.2 

3  .  556 

0.2812 

0.4967 

1.08G5 

113.3 

128 

346.2 

317.4 

1190.7 

873.3 

3  .  504 

0.2854 

0.4982 

1.0S37 

115.3 

130 

347.4 

318.6 

1191.0 

872.3 

3.452 

0.2897 

0.4998 

1.0809 

117.3 

132 

348.5 

319.9 

1191.2 

871.3 

3.402 

0.2939 

0.5013 

1.0782 

119.3 

134 

349.7 

321.1 

1191.5 

870.4 

3  .  354 

0.2981 

0  .  5028 

1.0755 

121.3 

136 

350.8 

322.3 

1191.7 

869.4 

3.308 

0.3023 

0.5043 

1.0728 

123.3 

138 

352.0 

323.4 

1192.0 

868.5 

3.263 

0  .  3065 

0  .  5057 

1.0702 

125.3 

140 

353.1 

324.6 

1192.2 

867.6 

3.219 

0.3107 

0.5072 

1.0675 

127.3 

142 

354.2 

325.8 

1192.5 

866.7 

3.175 

0.3150 

0.5086 

1.0649 

129.3 

144 

355.3 

326.9 

1192.7 

865.8 

3.133 

0.3192 

0.5100 

1.0624 

131.3 

146 

356.3 

328.0 

1192.9 

864.9 

3.092 

0.3234 

0.5114 

1.0599 

133.3 

148 

357.4 

329.1 

1193.2 

864  .  0 

3.052 

0.3276 

0.5128 

1.0574 

135.3 

150 

358.5 

330.2 

1193.4 

863.2 

3.012 

0.3320 

0.5142 

1.0550 

137.3 

152 

359.5 

331.4 

1193.6 

862.3 

2.974 

0  .  3362 

0.5155 

1.0525 

139.3 

154 

360.5 

332.4 

1193.8 

861.4 

2.938 

0  .  3404 

0.5169 

1.0501 

141.3 

156 

361.6 

333.5 

1194.1 

860  .  6 

2.902 

0.3446 

0.5182 

1.0477 

143.3 

158 

362.6 

334.6 

1194.3 

859  .  7 

2.868 

0.3488 

0.5195 

1.0454 

145.3 

160 

363.6 

335.6 

1194.5 

858.8 

2.834 

0.3529 

0  .  5208 

1.0431 

147.3 

162 

364.6 

336  .  7 

1194.7 

858.0 

2.801 

0  .  3570 

0.5220 

1  .  0409 

149.3 

164 

365.6 

337.7 

1194.9 

857.2 

2  .  769 

0.3612 

0.5233 

1.0387 

151.3 

166 

366.5 

338.7 

1195.1 

856.4 

2.737 

0.3654 

0  .  5245 

1.0365 

153.3 

168 

367  .  5 

339.7 

1195.3 

855.5 

2.706 

0.3696 

0  .  5257 

1.0343 

155.3 

170 

368.5 

340.7 

1195.4 

854.7 

2.675 

0.3738 

0.5269 

1.0321 

157.3 

172 

369.4 

341.7 

1195.6 

853  .  9 

2.645 

0.3780 

0.5281 

1.0300 

159.3 

174 

370.4 

342.7 

1195.8 

853.1 

2.616 

0  .  3822 

0.5293 

1.0278 

161.3 

176 

371.3 

343.7 

1196.0 

852.3 

2.588 

0.3864 

0.5305 

1.0257 

163.3 

178 

372.2 

344.7 

1196.2 

851.5 

2.560 

0  .  3906 

0.5317 

1  .  0235 

165.3 

180 

373.1 

345.6 

1196.4 

850.8 

2.533 

0.3948 

0  .  5328 

1.0215 

167.3 

182 

374.0 

346.6 

1196.6 

850.0 

2.507 

0  .  3989 

0.5339 

1.0195 

169.3 

184 

374.9 

347.6 

1196.8 

849.2 

2.481 

0.4031 

0.5351 

1.0174 

171.3 

186 

375.8 

348.5 

1196.9 

848.4 

2.455 

0.4073 

0.5362 

1.0154 

173.3 

188 

376.7 

349.4 

1197.1 

847.7 

2.430 

0.4115 

0.5373 

1.0134 

175.3 

190 

377.6 

350.4 

1197.3 

846.9 

2.406 

0.4157 

0  .  5384 

1.0114 

177.3 

192 

378.5 

351.3 

1197.4 

846.1 

2.381 

0.4199 

0.5395 

1.0095 

179.3 

194 

379.3 

352.2 

1197.6 

845.4 

2.358 

0.4241 

0.5405 

1.0076 

181.3 

196 

380.2 

353.1 

1197.8 

844.7 

2.335 

0.4283 

0.5416 

1  .  0056 

183.3 

198 

381.0 

354.0 

1197.9 

843  .  9 

2.312 

0.4325 

0  .  5426 

1.0038 

I 


408 


REEK. 


Properties  of  Saturated  Steam — Continued 


Total  Heat 

.• 

8  . 

above  32°  F. 

( 

a 

^J  nj 

& 

p 

leg1 

I* 

ii 

S     5 

1     j2 

j| 

.CO 

p*8 

o3 

Ca 

*o 

rt 
W 
*o 

PH   O 

"  8. 

sH 

b*           ^ 

4J          *C 

j 

-•.Q 

o  ™ 

£>* 

<U   ^ 

J3   ft 

SJ 

t> 

CO      ^ 

8s 

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o-  £ 

ft  g 

3  J3 

JJ3 

M 

-C*^  "d 

»c  ^  "S 

<D            g 

.S3  • 

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rt  ^j 

._) 

•/"fe 

-f->         O 

•*-*     <u 

ts  II  t> 

*O  G 

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185.3 

200 

381.9 

354.9 

1198.1 

843.2 

2.290 

0.437 

0.5437 

1.0019 

190.3 

205 

384.0 

357.1 

1198.5 

841.4 

2.237 

0.447 

0.5463 

0^9973 

195.3 

210 

386.0 

359.2 

1198.8 

839.6 

2.187 

0.457 

0.5488 

0.9928 

200.3 

215 

388.0 

361.4 

1199.2 

837.9 

2.138 

0.468 

0.5513 

0  .  9885 

205.3 

220 

389.9 

363.4 

1199.6 

836.2 

2.091 

0.478 

0  .  5538 

0.9841 

210.3 

225 

391.9 

365.5 

1199.9 

834.4 

2.046 

0.489 

0  .  5562 

0^9799 

215.3 

230 

393.8 

367.5 

1200.2 

832.8 

2.004 

0.499 

0  .  5586 

0.9758 

220.3 

235 

395.6 

369.4 

1200.6 

831.1 

1.964 

0  .  509 

0.5610 

0.9717 

225  .  3 

240 

397.4 

371.4 

1200.9 

829.5 

1.924 

0.526 

0  .  5633 

0.9676 

230.3 

245 

399.3 

373  .  3 

1201.2 

827.9 

1.887 

0.530 

0  5655 

0.9638 

235  .  3 

250 

401  .1 

375.2 

1201.5 

826.3 

1.850 

0.541 

0.5676 

0.9600 

245.3 

260 

404  .  5 

378.9 

1202.1 

823.1 

1.782 

0.561 

0  5719 

0.9525 

255  .  3 

270 

407.9 

382.5 

1202.6 

820.1 

1.718 

0.582 

0  .  5760 

0.9454 

265  .  3 

280 

411.2 

385.0 

1203.1 

817.1 

.658 

0.603 

0  .  5800 

0.9385 

275  .  3 

290 

414.4 

389.4 

1203.6 

814.2 

.602 

0.624 

0.5840 

0.9316 

285.3 

300 

417.5 

392.7 

1204.1 

811.3 

.551 

0.645 

0  .  5878 

0.9251 

295.3 

310 

420.5 

395.9 

1204.5 

808.5 

.502 

0.666 

0.5915 

0.9187 

305.3 

320 

423.4 

399.1 

1204.9 

805.8 

.456 

0  .  687 

0.5951 

0.9125 

315.3 

330 

426.3 

402.2 

1205.3 

803.1 

.413 

0.708 

0  .  5986 

0  .  9065 

325  .  3 

340 

429.1 

405.3 

1205.7 

800.4 

.372 

0.729 

0  .  6020 

0  .  9006 

335  .  3 

350 

431.9 

408.2 

1206.1 

797.8 

.334 

0  .  750 

0.6053 

0.8949 

315.3 

360 

434.6 

411.2 

1206.4 

795.3 

.298 

0.770 

0  .  6085 

0  .  8894 

355  .  3 

370 

437.2 

414.0 

1206.8 

792.8 

.264 

0.791 

0.6118 

0.8810 

3n5  .  3 

380 

439.8 

416.8 

1207.1 

790.3 

.231 

0.812 

0.6147 

0.8788 

375  .  3 

390 

442.3 

419.5 

1207.4 

787.9 

.200 

0.833 

0.6178 

0  .  8737 

385  .  3 

400 

444.8 

422 

1208 

786 

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0.86 

0.621 

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435  .  3 

450 

456.5 

435 

1209 

774 

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0.96 

0.635 

0.844 

485.3 

500 

467.3 

448 

1210 

762 

0.93 

1.08 

0.648 

0^822 

535  .  3 

550 

477.3 

459 

1210 

751 

0.83 

1.20 

0  659 

0   801 

585  .  3 

600 

486.6 

469 

1210 

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0.76 

1.32 

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AND    CONDENSERS'FOR   EVERY  SERVICE     ~~ldl 


E 

U  N 

I  0 

N 

STE 

AM 

P 

UM 

P 

c  o 

MPANY 

4 

Properties  of  Superheated  Steam 

(Condensed  from  Marks  and  Davis's  Steam  Tables  and  Diagrams.) 
••  specific  volume  in  cu.  ft.  per  lb.,  h  =  total  heat,  from  water  at  32°  F.  in  B.  T.  U. 
per  lb.,  n  =  entropy,  from  water  at  32°. 


5«  • 

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£JW 

ll 

62 
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Degrees  of  Superheat. 

0 

20 

59 

100 

150 

200 

250 

300 

400 

500 

20 

223.0 

v  20.08 

20.73 

21.69 

23.25 

24  .  80 

26.33 

27.85 

29  .  37 

32.39 

35  .  40 

h  11562 

1165.7 

1179.9 

1203.5 

1227.1 

1250.6 

1274.1 

1297.6 

1344  .  8 

1392.2 

n  1.7320 

1  .  7456 

1  .  7652 

1.7961 

1.8251 

1  .  8524 

1.8781 

1.9026 

1.9479 

1.9893 

40 

267.3 

v  10.49 

10.83 

11.33 

12.13 

12.93 

13.70 

14.48 

15.25 

16.78 

18.30 

h  1169.4 

1179.3 

1194.0 

1218.4 

1242.4 

1266.4 

1290.3 

1314.1 

1361.6 

1409.3 

n  1.6761 

1  .  6895 

1  .  7089 

1  .  7392 

1  .  7674 

1  .  7940 

1.8189 

1  .  8427 

1  .  8867 

1.9271 

60 

292.7 

v  7.17 

7.40 

7.75 

8.30 

8.84 

9.36 

9.89 

10.41 

11.43 

12.45 

h  1177.0 

1187.3 

1202.6 

1227.6 

1252.1 

1276.4 

1300.4 

1324.4 

1372.2 

1420.0 

n  1.6432 

1.6568 

1.6761 

1  .  7062 

1  .  7342 

1  .  7603 

1  .  7849 

1  .  8081 

1.8511 

1  .  8908 

80 

312.0 

v  5.47 

5.65 

5.92 

6.34 

6.75 

7.17 

7.56 

7.95 

8.72 

9.49 

h  1182.3 

1193.0 

1208.8 

1234.3 

1259.0 

1283.6 

1307.8 

1331.9 

1379.8 

1427.9 

n  1.6200 

1.6338 

1.6532 

1.6833 

1.7110 

1  .  7368 

1.7612 

1  .  7840 

1  .  8265 

1  .  8658 

100 

327.8 

v  4.43 

4.58 

4.79 

5.14 

5.47 

5.80 

6.12 

6.44 

7.07 

7.69 

h  1186.3 

1197.5 

1213.8 

1239.7 

1264.7 

1289.4 

1313.6 

1337.8 

1385.9 

1434.1 

n  1.6020 

1.6160 

1.6358 

1  .  6658 

1  .  6933 

1.7188 

1  .  7428 

1  .  7656 

1  .  8079 

1.8468 

120 

341.3 

v  3.73 

3.85 

4.04 

4.33 

4.62 

4.89 

5.17 

5.44 

5.96 

6.48 

h  1189.6 

1201.1 

1217.9 

1244.1 

1269.3 

1294  .  1 

1318.4 

1342.7 

1391.0 

1439.3 

n  1.5873 

1.6016 

1.6216 

1.6517 

1  .  6789 

.7041 

1  .  7280 

1  .  7505 

1  .  7924 

1.8311 

140 

353.1 

v  3.22 

3.32 

3.49 

3.75 

4.00 

4.24 

4.48 

4.71 

5.16 

5.61 

h  1192.2 

1204.3 

1221.4 

1248.0 

1273.3 

1298.2 

1322.6 

1346.9 

1395.4 

1443.8 

n  1.5747 

1  .  5894 

1.6096 

1.6395 

1.6686 

1  6916 

1.7152 

1  .  7376 

1  .  7792 

1.8177 

160 

363.6 

v  2.83  ' 

2.93 

3.07 

3.30 

3.53 

3.74 

3.95 

4.15 

4.56 

4.95 

h  1194.5 

1207.0 

1224.5 

1251.3 

1276.8 

1301.7 

1326.2 

1350.6 

1399.3 

1447.9 

n  1.5639 

1  .  5789 

1  .  5993 

1.6292 

1.6561 

1.6810 

1  .  7043 

1  .  7266 

1  .  7680 

1.8063 

180 

373.1 

v  2.53 

2.62 

2.75 

2.96 

3.16 

3.35 

3.54 

3.72 

4.09 

4.44 

h  1196.4 

1209.4 

1227.2 

1254.3 

1279.9 

1304.8 

1329.5 

1353.9 

1402.7 

1451.4 

n  1.5543 

i:5697 

1  .  5904 

1.6201 

1  .  6468 

1.6716 

1  .  6948 

1.7169 

1  .  7581 

1  .  7962 

200 

381.9 

v  2.29 

2.37 

2.49 

2.68 

2.86 

3  04 

3.21 

3.38 

3.71 

4.03 

h  1198.1 

1211.6 

1229.8 

1257.1 

1282.6 

1307.7 

1332.4 

1357.0 

1405.9 

1454.7 

n  1.5456 

1.5614 

1  .  5823 

1.6120 

1  .  6385 

1  .  6632 

1  .  6862 

1  .  7082 

1.7493 

1  .  7872 

220 

389.9 

v  2.09 

2.16 

2.28 

2.45 

2.62 

2.78 

2.94 

3.10 

3.40 

3.69 

h  1199.6 

1213.6 

1232.2 

1259.6 

1285.2 

1310.3 

1335.1 

1359.8 

1408.8 

1457.7 

1.5379 

1.5541 

1  .  5753 

1  .  6049 

1.6312 

1  .  6558 

1  .  6787 

1  .  7005 

1.7415 

1.7792 

210 

397.4 

1.92 

1.99 

2.09 

2.26 

2.42 

2.57 

2.71 

2.85 

3.13 

3.40 

1200.9 

1251.4 

1234.3 

1261.9 

1287.6 

312.8 

1337.6 

1362.3 

1411.5 

1400.5 

1  .  5309 

1  .  5476 

1.5690 

1  .  5985 

1.6246 

.6492 

.6720 

1.6937 

1  .  7344 

1.7721 

280 

404.5 

1.78 

1.84 

1.94 

2.10 

2.24 

2.39 

2.52 

2.65 

2.91 

3.16 

1202.1 

1217.1 

1236.4 

1264.1 

1289.9 

315.1 

340.0 

1364.7 

1414.0 

463.2 

1  .  5244 

1.5416 

1  .  5631 

1  .  5926 

1.6186 

.6430 

.6658 

1  .  6874 

1  .  7280 

1  .  7655 

280 

411.2 

1.66 

1.72 

1.81 

1.95 

2.09 

2.22 

2.35 

2.48 

2.72 

2.95 

h  1203.1 

1218.7 

1238.4 

1266.2 

1291.9 

317.2 

342.2 

1367.0 

1416.4 

1465.7 

n  1.5185 

1  .  5362 

1  .  5580 

1  .  5873 

1.6133 

.6375 

1  .  6603 

1.6818 

1  .  7223 

1  .  7597 

300 

417.5 

v  1.55 

1.60 

1.69 

1.83 

1.96 

2.09' 

2.21 

2.33 

2.55 

2.77 

h  1204.1 

1220.2 

1240.3 

1268.2 

1294.0 

319.3 

344.3 

1369.2 

1418.6 

1468.0 

n  1.5129 

1  .  5310 

1  .  5530 

1  .  5824 

1  .  6082 

.6323 

1  .  6550 

1.6765 

1.7168 

1.7541 

350 

431.9 

v  1.33 

1.38 

1.46 

1.58 

1.70 

.81 

1.92 

2.02 

2.22 

2.41 

h  1206.1 

1223.9 

1244.6 

1272.7 

1298.7 

324.1 

1349.3 

1374.3 

1424.0 

1473.7 

n  1.5002 

1.5199 

1  .  5423 

1.5715 

1.5971 

.6210 

1  .  6436 

1  .  6650 

1  .  7052 

1  .  7422 

400 

444.8 

v  1.17 

1.21 

1.28 

1.40 

1.50 

.60 

1.70 

1.79 

1.97 

2.14 

h  1207.7 

1227.2 

1248.6 

1276.9 

1303.0 

328.6 

1353.9 

1379.1 

1429.0 

1478.9 

n  1.4894 

1.5107 

1  .  5336 

1  .  5625 

1  .  5880 

.6117 

1  .  6342 

1  .  6554 

1  .  6955 

1  .  7323 

450 

456.5 

v  1.04 

1.08 

1.14 

1.25 

1.35 

.44 

1.53 

1.61 

1.77 

1.93 

h  1209 

1231 

1252 

1281 

1307 

333 

1358 

1383 

1434 

1484 

n  1.479 

1.502 

1.526 

1.554 

1.580 

.603 

1.626 

1.647 

1.687 

1.723 

500 

467.3 

v  0.93 

0.97 

1.03 

1.13 

1.22 

.31 

1.39 

1.47 

1.62 

1.76 

h  1210 

1233 

1256 

1285 

1311 

337 

1362 

1388 

1438 

1489 

n  1.470 

1.496 

1.519 

1.548 

1.573 

.597 

1.619 

1.640 

1.679 

1.715 

PUMPING    MACHINERY.    AIR.   COMPRESSORS 


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AND    CONDENSERS    FOR    EVERY  SERVICE 


411 


1  UNB 

I  ON 

STEAM 

P  UM  P 

COM  PANY      H| 

U.  S.  Standard 

Schedule  of  Standard  Flanges 

1  inch  to  40  inches,  inclusive. 
For  Steam  Pressures  up  to  125  Ibs.  per  square  inch. 


Size    of 
Pipe 

Diameter 
of  Flange 

Thickness 
of  Flange 

Diameter 
of  Bolt 
Circle 

Number 
of  Bolts 

Size    of 
Bolts 

Diameter 
of  Bolt 
Holes 

1 

4 

7  . 

3 

4 

TT 

A 

1% 

4K 

K 

3% 

4 

iV 

A 

IK 

5 

A 

3j/8 

4 

A 

2 

6 

K 

4% 

4 

% 

2K 

7 

5K 

4 

% 

% 

3 

7K 

% 

6   " 

4 

H 

% 

3K 

8K 

i! 

7 

4 

% 

% 

4 

9 

li 

7K 

8 

% 

% 

41/2 

9M 

if 

7M 

8 

M 

K 

5 

10 

le5 

8K 

8 

% 

/"8 

6 

11 

1 

9K 

8 

% 

7^ 

7 

12K 

lyV 

10% 

8 

M 

K 

8 

13K 

IJi 

11% 

8 

^ 

9 

15 

1^8 

13% 

12 

% 

10 

16 

IT\ 

14% 

12 

% 

i 

12 

19 

17 

12 

Ys 

i 

14 

21 

13/8 

18% 

12 

iH 

15 

22% 

l3/^ 

20 

16 

i 

16 

23K 

** 

21% 

16 

i 

IK 

18 

25 

22% 

16 

1^8 

1% 

20 

27  K 

111 

25 

20 

IJ/g 

1;% 

22 

29  K 

27% 

20 

IK 

13/S 

24 

32 

J-/Jf 

29  K 

20 

1% 

1^8 

26 

34% 

2 

31% 

24 

1% 

I/7/ 

28 

36K 

2iV 

34 

28 

1% 

]3// 

30 

38% 

2K 

36 

28 

l/^ 

IK 

32 

41% 

2% 

38K 

28 

IK 

1?-^ 

34 

43% 

2A 

40K 

32 

IK 

i/^ 

36 

46 

42% 

32 

iK 

154 

38 

48% 

2//8 

45% 

32 

i/^ 

1% 

40 

50% 

2M 

47% 

36 

^ 

iM 

i 

ATT 

LE 

C 

RE 

EK. 

MICHIGAN. 

U. 

S. 

A. 

11 

U.  S.  Standard 

Schedule  of  Extra  Heavy  Flanges 

1  inch  to  48  inches,  inclusive 
For  Steam  Pressures  from  125  to  250  Ibs.  per  square  inch. 


Size 
of 
Pipe 

Diameter 
of 
Flange 

Thickness 
of 
Flange 

Diameter 
of  Bolt 
Circle 

Number 
of 
Bolts 

Size 
of 
Bolts 

Diameter 
of  Bolt 
Holes 

1 

4l/2 

3M 

4 

1A 

K 

1/4 

5  " 

r 

3/4 

4 

K 

K 

IK 

6 

4 

4^ 

4 

K 

2 

6K 

K 

5 

4 

H 

% 

2^ 

71^ 

i 

^K 

4 

3  " 

8/4 

IK 

6K 

8 

% 

r 

3K 

9 

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7M 

8 

% 

K 

4 

10 

1M 

7% 

8 

% 

K 

4K 

IOK 

llV 

8^/2 

8 

% 

K 

5 

iix' 

»H 

9M 

8 

% 

K 

6 

12J/2 

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IOK 

12 

% 

K 

7 

14 

IK 

n'K 

12 

^ 

i 

8 

15 

IK 

13 

12 

i 

9 

16J4 

l-Ji 

14 

12 

i 

IK 

10 

17M 

IK 

15J4 

16 

i 

IK 

12 

2 

17% 

16 

iJi 

1^4 

14 

23   2 

2^8 

20J4 

20 

m 

IK 

15 

24^ 

2vV 

21K 

20 

1^ 

16 

25M 

22^ 

20 

IM 

«< 

18 

•-28 

2K 

24% 

24 

1^ 

iK 

20 

30K 

2K 

27 

24 

22 

33 

2K 

29M 

24 

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i^l 

24 

36 

2^£ 

32 

24 

IK 

1% 

26 

38^ 

211 

34K 

28 

IK 

1% 

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40% 

2U 

37  ' 

28 

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1% 

30 

43' 

3 

39J4 

28 

1% 

IK 

32 

45J4 

3K 

41K 

28 

IK 

2 

34 

47^ 

3M 

43M 

28 

IK 

2 

36 

50 

3K 

46 

32 

IK 

2 

38 

52J4 

3iV 

48 

32 

iK 

2 

40 

54^ 

SiV 

5°^ 

36 

IK 

2 

42 

57 

3U 

36 

IK 

2 

44 

59J/4 

55 

36 

2 

2K 

46 

•  61K 

3K 

57M 

40 

2 

2K 

48 

65 

4 

60% 

40 

2 

2K 

413 


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a! 


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i  w  «  ^  «o  oo  o  eo  «  c  •*  «  ^  o  So  cs  o  o?  o  o  c->oci «  w  c-j  N 


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BATTLE       CREEK 


Extra  Strong  Pipe— Black  and  Galvanized 

All  Weights  and  Dimensions  are  Nominal 


Size 

Diameters 

Thickness 

Weight 
per  foot 
Plain    Ends 

External 

Internal 

1A 

.405 

.215 

.095 

.314 

M 

.540 

.302 

.119 

.535 

y8 

.675 

.423 

.126 

.738 

H 

.840 

.546 

.147 

1.087 

% 

1.050 

.742 

.154 

1.473 

l 

1.315 

.957 

.179 

2.171 

1M 

1.660 

1.278 

.191 

2.996 

m 

1.900 

1.500 

.200 

3.631 

2 

2.375 

1.939 

.218 

5.022 

2H 

2.875 

2.323 

.276 

7.661 

3 

3.500 

2.900 

.300 

10.252 

3^ 

4.000 

3.364 

.318 

12.505 

4 

4.500 

3.826 

.337 

14.983 

4K 

5.000 

4.290 

.355 

17.611 

5 

5.563 

4.813 

.375 

20.778 

6 

6.625 

5.761 

.432 

28.573 

7 

7.625 

6.625 

.500 

38  048 

8 

8.625 

7.625 

.500 

43.388 

9 

9.625 

8.625 

.500 

48.728 

10 

10.750 

9.750 

.500 

54.735 

11 

11.750 

10.750 

.500 

60.075 

12 

12.750 

11.750 

.500 

65.415 

13 

14.000 

13  .  000 

.500 

72.091 

14 

15.000 

14.000 

.500 

77.431 

15 

16.000 

15.000 

.500 

82.771 

Double  Extra  Strong  Pipe— Black  and  Galvanized 

All  Weights  and  Dimensions  are  Nominal 


Size 

Diameters 

Thickness 

Weight 
per  foot 
Plain    Ends 

External 

Internal 

H 

H 
1 

1M 

.840 
1.050 
1.315 
1.660 

.252 
.434 
.599 
.896 

.294 
.308 
.358 
.382 

1.714 
2.440 
3.659 
5.214 

iy2 

2 

2l/2 

3 

1.900 
2.375 

2.875 
3.500 

1.100 
1.503 
1.771 
2.300 

.400 
.436 
.552 
.600 

6.408 
9.029 
13.695 

18.583 

Zl/2 

4 
4^ 
5 

4.000 
4.500 
5.000 
5.563 

2.728 
3.152 
3.580 
4.063 

.636 
.674 
.710 
.750 

22.850 
27.541 
32.530 
38.552 

6 

7 
8 

6.625 
7.625 
8.625 

4.897 
5.875 
6.875 

.864 

.875 
.875 

53  160 
63  .  079 
72.424 

j|        AN  D    C  6  N  D  E  N  S  E  R  S    FORE  V  E  RV"s"ER.VT^E^  T 

415 


UNION       STEAM       PUMP       COMPANY 


Contents  of  Round  Tanks  in  U.  S.  Gallons, 
for  Each  Foot  in  Depth 


Dia- 
meter 
Ft.  In. 

Gallons, 
1  Foot  in 
Depth 

Dia- 
meter 
Ft.  In. 

Gallons, 
1  Foot  in 
Depth 

Dia- 
meter 
Ft.'  In. 

Gallons, 
1    Foot   in 
Depth 

1     0 

5.8735 

11     0 

710.6977 

21     0 

2590.2290 

1     3 

9.1766 

11     3 

743  .  3686 

21     3 

2652.2532 

1     6 

13.2150 

11     6 

776.7746 

21     6 

2715.0413 

1     9 

17.9870 

11     9 

810.9143 

21     9 

2778.5486 

2     0 

23.4940 

12     0 

848  .  1890 

22     0 

2842.7910 

2     3 

29.7340 

12     3 

881.3966 

22     3 

2907.7664 

2     6 

36.7092 

12     6 

917.7395 

22     6 

2973.4889 

2     9 

44.4179 

12     9 

954.8159 

22     9 

3039  .  9209 

3     0 

52.8618 

13     0 

992.6274 

23     0 

3107.1001 

3     3 

62.0386 

13     3 

1031.1719 

23     3 

3175.0122 

3     6 

73.1504 

13     6 

1070.4514 

23     6 

3243  .  6595 

3     9 

82  .  5959 

13     9 

1108.0645 

23     9 

3313.0403 

4     0 

93.9754 

14     0 

1151.2129 

24     0 

3383.1563 

4     3 

106.1290 

14     3 

1192.6940 

24     3 

3454.0051 

4     6 

118.9386 

14     6 

1234.9104 

24     6 

3525.5929 

4     9 

132.5209 

14     9 

1277.8615 

24     9 

3597.9068 

5     0 

146.8384 

15     0 

1321.5454 

25     0 

3670.9596 

5     3 

161.8886 

15     3 

1365.9634 

25     3 

3744.7452 

5     6 

177.6740 

15     6 

1407.5165 

25     6 

3819.2657 

5     9 

194.1913 

1  15     9 

1457.0032 

25     9 

3894  .  5203 

6     0 

211.4472 

16     0 

1503.6250 

26     0 

3970  .  5098 

6     3 

229.4342 

!  16     3 

1550.9797 

26     3 

4047.2322 

6     6 

248.1564 

i  16     6 

1599.0696 

26     6 

4124.6898 

6     9 

267.6122 

16     9 

1647.8930 

26     9 

4202.9610 

7     0 

287.8032 

17     0 

1697.4516 

27     0 

4281.8072 

7     3 

308.7270 

17     3 

1747.7431 

27     3 

4361.4664 

7     6 

330.3859 

17     6 

1798  .  7698 

27     6 

4441.8607 

7     9 

352.7665 

17     9 

1850.5301 

27     9 

4522.9886 

8     0 

375.9062 

18     0 

1903.0254 

28     0 

4604.8517 

8     3 

399.7666 

18     3 

1956.2537 

28.    3 

4686.4876 

8     6 

424  .  3625 

18     6 

2010.2171 

28     6 

4770.7787 

8     9 

449.2118 

18     9 

2064.9140 

28     9 

4854.8434 

i 

PUMPING    MACHINERY,    AIR    COMPRESS 


416 


C  RE  E  K ~~     MICH  I  G  AN .      U.  S.  A. 


Horse  Power  of  an  Engine 

a  =  Area  of  the  piston  in  square  inches. 

p  =  Mean  effective  pressure  of  the  steam  on  the  piston  per  square  inch. 

v  =  Velocity  of  piston  per  minute. 

a  X  p  X  v 
Then  H.  P.  =  - 

'       33,000 
The  mean  pressure  in  the  cylinder  when  cutting  off  at 

\i  stroke  =  bo  er  pressure  multiplied  by  .597 
lA      "       =  '   .670 

.743 

V2      "       =  ,847 

.919 
.937 
.966 
.992 

To  find  the  diameter  of  a  cylinder  of  an  engine  of  a  required  nominal  horse- 
power: 

5500 

multiplied  by  H.  P.  =  a. 


Ranges  in  Steam  Consumption  by  Prime  Movers 


Type  Engine 

Saturated 
Steam  Lbs. 
per  Hour 

100° 

Super  Lbs. 
per  Hour 

200° 
Super  Lbs. 
per  Hour 

Simple  —  Non-condensing  
Simple  —  Non-condensing    auto- 
matic                               

29—45 
26—40 

20—38 
18—34 

18—35 
16—30 

Simple  —  Non-condensing  Corliss  . 
Compound  —  Non-condensing.  .  .  . 
Compound  —  Condensing  

26—35 
19—28 
12—22 

18—30 
15—25 
10—20 

±3—  22 
9—17 

Turbines  Non-condensing 
(K.  W.  Hr.)  

28—60 

24—54 

21—48 

Turbines  Condensing  (K.  W.  Hr.) 

12—42 

10—38 

9—31 

AND    CONDEN  S  ERS    FOR    EVERY   5  ERVIC E 


STEAM 


--j:--.  •>  aa^a^BK 
PUMP 


COM  PANY 


Different  Standards  for  Wire  Gauge  in  Use 
in  the  United  States 

Dimensions  of  sizes  in  Decimal  Parts  of  an  Inch 


Number  of 
Wire  Gauge 

American  or 
Brown  & 
Sharpe 

Birmingham 
or  Stub's  Wire 

Washburn  & 
MoenMfg.Co. 
Worcester, 
Mass. 

Imperial 
Wire  Gauge 

<a 
f 
m  & 
t« 
CO 

U.  S. 
Standard 
for  Plate 

Number  of 
Wire  Gauge 

000000 

.46i 

.46875 

000000 

00000 

.432 

.4375 

00000 

0000 

.46 

.454 

3938 

.400 

.40025 

0000 

000 

.40964 

.425 

.3625 

.372 

.375 

000 

00 

.3648 

.38 

.3310 

.318 

.34375 

00 

0 

.32486 

.34 

.3065 

.324 

.3125 

0 

1 

.2893 

.3 

.2830 

.300 

.227 

.28125 

1 

2 

.25763 

.284 

.2625 

.276 

.219 

.265625 

2 

3 

.22942 

.259 

.2437 

.252 

.212 

.25 

3 

4 

.20431 

.238 

.2253 

.232 

.207 

.234375 

4 

5 

.18194 

.22 

.2070 

.212 

.204 

.21875 

5 

6 

.  16202 

.203 

.1920 

.192 

.201 

.203125 

6 

7 

.  14428 

.18 

.1770 

.176 

.199 

.1875 

7 

8 

.  12849 

.165 

.1620 

.160 

.197 

.171875 

8 

9 

.11443 

.148 

.1483 

.144 

.194 

.15625 

9 

10 

.10189 

.134 

.1350 

.128 

.191 

.  140625 

10 

11 

.090742 

.12 

.1205 

.116 

.188 

.125 

11 

12 

.080808 

.109 

.1055 

.104 

.185 

.109375 

12 

13 

.071961 

.095 

.0015 

.092 

.182 

.09375 

13 

14 

.064084 

.083 

.0800 

.080 

.180 

.078125 

14 

15 

.057068 

.072 

.0720 

.072 

.178 

.0708125 

15 

16 

.05082 

.065 

.0625 

.064 

.175 

.0625 

16 

17 

.045257 

.058 

.  0540 

.056 

.172 

.05625 

17 

18 

.  040303 

.049 

.0475 

.048 

.168 

.05 

18 

19 

.03589 

.042 

.0410 

.040 

.164 

.04375 

19 

20 

.031961 

.035 

.0348 

.036 

.161 

.0375 

20 

21 

.028462 

.032 

.03175 

.032 

.157 

.034375 

21 

22 

.025347 

.028 

.0286 

.028 

.155 

.03125 

22 

23 

.022571 

.025 

.0258 

.024 

.153 

.028125 

23 

24 

.0201 

.022 

.0230 

.022 

.151 

.025 

24 

25 

.0179 

.02 

.0204 

020 

.148 

.021875 

25 

26 

.01594 

.018 

.0181 

.018 

.146 

.01875 

26 

27 

.014195 

.016 

.0173 

.0164 

.143 

.0171875 

27 

28 

.012641 

.014 

.0162 

.0149 

.139 

.015625 

28 

29 

.011257 

.013 

.0150 

.0136 

.134 

.0140625 

29 

30 

.010025 

.012 

.0140 

.0124 

.127 

.0125 

30 

31 

.008928 

.01 

.0132 

.0116 

.120 

.0109375 

31 

32 

.00795 

.009 

.0128 

.0108 

.115 

.01015625 

32 

33 

.00708 

.008 

.0118 

.0100 

.112 

.009375 

33 

34 

.006304 

.007 

.0104 

.0092 

.110 

.00859375 

34 

35 

.005614 

.005 

.0095 

.0084 

.108 

.0078125 

35 

36 

.005 

.004 

.0090 

.0076 

.106 

.00703125 

36 

37 

.004453 

.0068 

.103 

.  006640625 

37 

38 

.003965 

]0060 

ilOl 

.  00625 

38 

39 

.003531 

...... 

.0052 

.099 

39 

40 

.003144 

.0048 

.007 

40 

PUMPING    MACHINERY,    AIR   COMPRESJ 


418 


Logarithms  of  Numbers  from  0  to  1000 


No. 

0 

1 

2 

3 

4 

5 

.  6 

7 

8 

9 

0 

0 

00000 

30103 

47712 

60206 

69  89  7 

77815 

84510 

90309 

95424 

10 

00000 

00432 

00860 

01284 

01703 

02119 

02531 

02938 

03342 

03743 

11 

04139 

04532 

04922 

05308 

05690 

06070 

06446 

06819 

07188 

07555 

12 

07918 

08279 

08636 

08991 

09342 

09691 

10037 

10380 

10721 

11059 

13 

11394 

11727 

12057 

12385 

12710 

13033 

13354 

13672 

13988 

14301 

14 

14613 

14922 

15229 

15534 

15836 

16137 

16135 

16732 

17026 

17319 

15 

17609 

17898 

18184 

18469 

18752 

19033 

19312 

19590 

19866 

20140 

16 

20412 

20683 

20952 

21219 

21484 

21748 

22011 

22272 

22531 

22789 

17 

23045 

23300 

23553 

23805 

24055 

21304 

24551 

24797 

25042 

25285 

18 

25527 

25768 

26007 

26245 

26482 

26717 

26951 

27184 

27416 

27646 

19 

27875 

28103 

28330 

28556 

28780 

29003 

29226 

29447 

29667 

29885 

20 

30103 

30320 

30535 

30750 

30963 

31175 

31387 

31597 

31806 

32015 

21 

32222 

32428 

32634 

32838 

33041 

33244 

33445 

33646 

33846 

34044 

22 

34242 

34439 

34635 

34830 

35025 

35218 

35411 

35603 

35793 

35984 

23 

36173 

36361 

36549 

36736 

36922 

37107 

37291 

37475 

37658 

37810 

24 

38021 

38202 

38382 

38561 

38739 

38917 

39094 

39270 

39445 

39620 

25 

39794 

39967 

40140 

40312 

40483 

40654 

40824 

40993 

41162 

41330 

26 

41497 

41664 

41830 

41996 

42160 

42325 

42488 

42651 

42813 

42975 

27 

43136 

43297 

43457 

43616 

43775 

43933 

44091 

44248 

44404 

44560 

28 

44716 

44871 

45025 

45179 

453'32 

45484 

45637 

45788 

45939 

46090 

29 

46240 

46389 

46538 

46687 

46835 

46982 

47129 

47276 

47422 

47567 

30 

47712 

47857 

48001 

48144 

48287 

48430 

48572 

48714 

48855 

48996 

31 

49136 

49276 

49415 

49554 

49693 

49831 

49969 

50106 

50243 

50379 

32 

50515 

50651 

50786 

50920 

51055 

51188 

51322 

51455 

51587 

51720 

33 

51851 

51983 

52114 

52244 

52375 

52504 

52633 

52763 

52S92 

53020 

34 

53148 

53275 

53403 

53529 

53656 

53782 

53908 

54033 

54158 

54283 

35 

54407 

54531 

54654 

54777 

54900 

55023 

55145 

55267 

55388 

55509 

36 

55630 

55751 

55871 

55991 

56110 

56229 

56348 

56467 

56585 

56703 

37 

56820 

56937 

57054 

57171 

57287 

57403 

57519 

57634 

57749 

57864 

38 

57978 

58093 

58206 

58320 

58433 

58546 

58659 

58771 

58883 

58995 

39 

59106 

59218 

59329 

59439 

59550 

59660 

59770 

59879 

59988 

60097 

40 

60206 

60314 

60423 

60531 

60638 

60746 

60853 

60959 

61066 

61172 

41 

61278 

61384 

61490 

61595 

61700 

61805 

61909 

62014 

62118 

62221 

42 

62325 

62428 

62531 

62634 

62737 

62839 

62941 

63043 

63144 

63246 

43 

63347 

63448 

63548 

63649 

63749 

63849 

63949 

64048 

64147 

64246 

44 

64345 

64444 

64542 

64640 

64738 

64836 

64933 

65031 

65128 

65225 

45 

65321 

65418 

65514 

65610 

65706 

65801 

65896 

65992 

66087 

66181 

46 

66276 

66370 

66464 

66558 

66652 

66745 

66839 

66932 

67025 

67117 

47 

67210 

67302 

67394 

67486 

67578 

67669 

67761 

67852 

67943 

68034 

48 

68124 

68215 

68305 

68395 

68485 

68574 

68664 

68753 

68842 

68931 

49 

69020 

69108 

69197 

69285 

69373 

69461 

69548 

69636 

69723 

69810 

50 

69897 

69984 

70070 

70157 

70243 

70329 

70415 

70501 

70586 

70672 

51 

70757 

70842 

70927 

71012 

71096 

71181 

71265 

71349 

71433 

71517 

52 

71600 

71684 

71767 

71850 

71933 

72016 

72099 

72181 

72263 

72346 

53 

72428 

72509 

72591 

72673 

72754 

72835 

72916 

72997 

73078 

73153 

54 

73239 

73320 

73400 

73480 

73560 

73640 

73719 

73799 

73878 

73957 

419 


Logarithms  of  Numbers,  from  0  to  1000 — 
Continued 


No. 

O 

2 

55 

74036 

74115 

74194 

74273 

74351 

74429 

74507 

74586 

74663 

74741 

56 

.74819 

74896 

74974 

75051 

75128 

75205 

75282 

75358 

75435 

75511 

57 

75587 

75664 

75740 

75815 

75891 

75967 

76042 

76118 

76193 

76268 

58 

76343 

76418 

76492 

76567 

76641 

76716 

76790 

76864 

76938 

77012 

59 

77085 

77159 

77232 

77305 

77379 

77452 

77525 

77597 

77670 

77743 

60 

77815 

77887 

77960 

78032 

78104 

78176 

78247 

78319 

78390 

78462 

61 

78533 

78604 

78675 

78746 

78817 

78888 

78958 

79029 

79099 

79169 

62 

79239 

79309 

79379 

79449 

79518 

79588 

79657 

79727 

79796 

79865 

63 

79934 

80003 

80072 

80140 

80209 

80277 

S0346 

80414 

80482 

80550 

64 

80618 

80686 

80754 

80821 

80889 

S0956 

81023 

81090 

81158 

S1224 

65 

81291 

81358 

81425 

81491 

81558 

81624 

81690 

81756 

81823 

81889 

66 

81954 

82020 

82086 

82151 

82217 

82282 

82347 

82413 

82478 

82543 

67 

82607 

82672 

82737 

82802 

82866 

82930 

82995 

83059 

83123 

83187 

68 

83251 

83315 

83378 

83442 

83506 

83569 

83632 

83696 

83759 

83822 

69 

83885 

83948 

84011 

84073 

84136 

84198 

84261 

84323 

84386 

84448 

70 

84510 

84572 

84634 

84696 

84757 

84819 

84880 

84942 

85003 

85065 

71 

85126 

85187 

85248 

85309 

85370 

85431 

85491 

85552 

85612 

85673 

72 

85733 

85794 

85854 

85914 

85974 

86034 

86094 

86153 

86213 

86273 

73 

86332 

86392 

86451 

86510 

86570 

86629 

86688 

86747 

86806 

86864 

74 

86923 

86982 

87040 

87099 

87157 

87216 

87274 

87332 

87390 

S7448 

75 

87506 

87564 

87622 

87680 

87737 

87795 

87852 

87910 

87967 

88024 

76 

88081 

88138 

88196 

88252 

88309 

88366 

88423 

88480 

88536 

88593 

77 

88649 

88705 

88762 

88818 

88874 

88930 

88986 

89042 

89098 

89154 

78 

89209 

89265 

89321 

89376 

89432 

89487 

89542 

89597 

89653 

89708 

79 

89763 

89818 

89873 

89927 

89982 

90037 

90091 

90146 

90200 

90255 

80 

90309 

90363 

90417 

90472 

90526 

90580 

90634 

90687 

90741 

90795 

81 

90849 

90902 

90956 

91009 

91062 

91116 

91169 

91222 

91275 

91328 

82 

91381 

91434 

91487 

91540 

91593 

91645 

91698 

91751 

91803 

91855 

83 

91908 

91960 

92012 

92065 

92117 

92169 

92221 

92273 

92324 

923J6 

84 

92428 

92480 

92531 

92583 

92634 

92686 

92737 

92788 

92840 

92891 

85 

92942 

92993 

93044 

93095 

93146 

93197 

93247 

93298 

93349 

93399 

86 

93450 

93500 

93551 

93601 

93651 

93702 

93752 

93802 

93852 

93902 

87 

93952 

94002 

94052 

94101 

94151 

94201 

942.50 

94300 

94349 

94399 

88 

94448 

94498 

94547 

94596 

94645 

94694 

94743 

94792 

94841 

94890 

89 

94939 

94988 

95036 

95085 

95134 

95182 

95231 

95279 

95328 

95376 

90 

95424 

95472 

95521 

95569 

95617 

95665 

95713 

95761 

95809 

95856 

91 

95904 

95952 

95999 

96047 

96095 

96142 

96190 

96237 

96284 

96332 

92 

96379 

96426 

96473 

96520 

96567 

96614 

96661 

96708 

96755 

96802 

93 

96848 

96895 

96942 

96988 

97035 

97081 

97128 

97174 

97220 

97267 

94 

97313 

97359 

97405 

97451 

97497 

97543 

97589 

97635 

97681 

97727 

95 

97772 

97818 

97864 

97909 

97955 

98000 

98046 

98091 

98137 

98182 

96 

98227 

98272 

98318 

98363 

98408 

98453 

98498 

98543 

98588 

98632 

97 

98677 

98722 

98767 

98811 

98856 

98900 

98945 

98989 

99034 

99078 

98 

99123 

99167 

99211 

99255 

99300 

99344 

99388 

99432 

99476 

99520 

99 

99564 

99607 

99651 

99695 

99739 

99782 

99826 

99870 

99913 

99957 

420 


Natural  Trigonometrical  Functions 


0 

M. 

Sine. 

Co-vers. 

Co-sec- 

Tang. 

Cc-tan. 

Secant. 

Ver.Sin. 

Co-sine 

0 

0 

15 

.00000 
.00430 

1  .  00000 
.99564 

.nfinite 
229  .  18 

.00000 
.00436 

Infinite 
229  .  18 

1  .  0000 
1.0000 

.00000 
.00001 

1.00000 
.99999 

90 

0 

45 

30 

.00873 

.99127 

114.59 

.00873 

114.59 

1.0000 

.00004 

.99996 

30 

45 

.01309 

.98691 

76  .  397 

.01309 

76  .  390 

1.0001 

.00009 

.99991 

15 

1 

0 

.01745 

.98255 

57  .  299 

.01745 

57  .  290 

1.0001 

.00015 

.99985 

89 

0 

15 

.02181 

.97819 

45.840 

.02182 

45.829 

1.0002 

.00024 

.99976 

45 

30 

.02618 

.97382 

38  .  202 

.02618 

38.188 

1.0003 

.00034 

.99966 

3J 

45 

.03054 

.96946 

32.746 

.03055 

32  .  730 

1.0005 

.00047 

.99953 

15 

2 

0 

.03490 

.96510 

28.654 

.03492 

28  .  636 

1.0006 

.00061 

.99939 

88 

0 

15 

.03926 

.96074 

25.471 

.03929 

25.452 

1.0008 

.00077 

.99923 

45 

30 

.04362 

.95638 

22.926 

.04366 

22  .  904 

1.0009 

.00095 

.99905 

30 

45 

.04798 

.95202 

20  .  843 

.04803 

20.819 

1.0011 

.00115 

.99885 

15 

3 

0 

.05234 

.94766 

19.107 

.05241 

19.081 

1.0014 

.00137 

.99863 

87 

0 

15 

.05669 

.94331 

17.639 

.05678 

17.611 

1.0016 

.00161 

.99839 

45 

30 

.06105 

.93895 

16.380 

.06116 

16.350 

1.0019 

.00187 

.99813 

30 

45 

.06540 

.93460 

15.290 

.06554 

15.527 

1.0021 

.00214 

.99786 

15 

4 

0 

.06976 

.93024 

13.336 

.06993 

14.301 

1.0024 

.00244 

.99756 

86 

0 

15 

.07411 

.92589 

13.494 

.07431 

13.457 

1  .  0028 

.00275 

.99725 

45 

30 

.07846 

.92154 

12.745 

.07870 

12.706 

1.0031 

.00308 

.99692 

30 

45 

.08281 

.91719 

12.076 

.08309 

12.035 

1.0034 

.00343 

.99656 

15 

5 

0 

.08716 

.91284 

11.474 

.08749 

11.430 

1.0038 

.00381 

.99619 

85 

0 

15 

.09150 

.90850 

10.929 

.09189 

10.883 

1.0042 

.00420 

.99580 

45 

30 

.09585 

.90415 

10.433 

.09629 

10.385 

1  .  0046 

.  00460 

.99540 

30 

45 

.10019 

.89981 

9.9812 

.  10069 

9.9310 

1.0051 

.00503 

.99497 

15 

6 

0 

.  10453 

.89547 

9.5668 

.10510 

9.5144 

1.0055 

.00548 

.99452 

84 

0 

15 

.10887 

.89113 

9.1855 

.  10952 

9.1309 

1.0060 

.00594 

.99406 

45 

30 

.11320 

.88680 

8.8337 

.11393 

8.7769 

1.0065 

.00643 

.99357 

30 

45 

.11754 

.88246 

8.5079 

.11836 

8.4490 

1.0070 

.00693 

.99307 

15 

7 

0 

.12187 

.87813 

8.2055 

.12278 

8.1443 

1.0075 

.00745 

.99255 

83 

0 

15 

.12620 

.  87380 

7.9240 

.12722 

7  .  8606 

1.0081 

.00800 

.99200 

45 

30 

.  13053 

.86947 

7.6613 

.13165 

7.5958 

1.0086 

.00856 

.99144 

30 

45 

.13485 

.86515 

7.4156 

.13609 

7.3479 

1.0092 

.00913 

.99086 

15 

8 

0 

.13917 

.86083 

7.1853 

.  14054 

7.1154 

1.0098 

.00973 

.99027 

82 

0 

15 

.  14349 

.85651 

6.9690 

.14199 

6.8969 

1.0105 

.01035 

.98965 

45 

30 

.11781 

.85219 

6.7655 

.  14945 

6.6912 

1.0111 

.01098 

.98902 

30 

45 

.15212 

.84788 

6.5736 

.15391 

6.4971 

1.0118 

.01164 

.98836 

15 

9 

0 

.15643 

.84357 

6.3924 

.  15838 

6.3138 

1.0125 

.01231 

.98769 

81 

0 

15 

.  16074 

.83926 

6.2211 

.16286 

6.1402 

1.0132 

.01300 

.98700 

45 

30 

.16505 

.83495 

6.0589 

.  16734 

5.9758 

1.0139 

.01371 

.98629 

30 

45 

.16935 

.83065 

5.9049 

.17183 

5.8197 

1.0147 

.01444 

.98556 

15 

10 

0 

.17365 

.82635 

5  .  7588 

.  17633 

5.6713 

1.0154 

.01519 

.98481 

80 

0 

15 

.17794 

.82206 

5.6198 

.  18083 

5.5301 

1.0162 

.01596 

.98404 

45 

30 

.18224 

.81776 

5.4874 

.18534 

5.3955 

1.0170 

.01675 

.98325 

30 

45 

.  18652 

.81348 

5.3612 

.  18986 

5.2672 

1.0179 

.01755 

.98245 

15 

11 

0 

.19081 

.80919 

5.2408 

.  19438 

5.1446 

1.0187 

.01837 

.98163 

79 

0 

15 

.19509 

.80491 

5.1258 

.19891 

5.0273 

1.0196 

.01921 

.98079 

45 

30 

.19937 

.80063 

5.0158 

.20345 

4.9152 

1.0205 

.02008 

.97992 

30 

45 

.  20364 

.  79636 

4.9106 

.20800 

4.8077 

1.0214 

.02095 

.97905 

15 

12 

0 

.20791 

.79209 

4.8097 

.21256 

4.7046 

1.0223 

.02185 

.97815 

78 

0 

15 

.21213 

.78782 

4.7130 

.21712 

4  .  6057 

1.0233 

.02277 

.97723 

45 

30 

.21644 

.  78356 

4  .  6202 

.22169 

4.5107 

1.0243 

.02370 

.97630 

30 

45 

.  22070 

.77930 

4.5311 

.22628 

4.4194 

1.0253 

.02466 

.97534 

15 

13 

0 

.22495 

.  77505 

4.4454 

.23087 

4.3315 

1.0263 

.02563 

.97437 

77 

0 

15 

.22920 

.77080 

4  .  3630 

.23547 

4  .  2468 

1.0273 

.02662 

.97338 

45 

30 

.23345 

.76655 

4.2837 

.  24008 

4.1653 

1  .  0284 

.02763 

.97237 

30 

45 

.23769 

.76231 

4.2072 

.24470 

4.0867 

1.0205 

.02866 

.97134 

15 

14 

0 

.24192 

.75808 

4.1336 

.24933 

4.0108 

1  .  0306 

.02970 

.97030 

76 

0 

15 

.24615 

.  75385 

4  .  0625 

.25397 

3.9375 

1.0317 

.03077 

.96923 

45 

30 

.25038 

.74962 

3.9939 

.25862 

3.8667 

1.0329 

.03185 

.96815 

30 

45 

.  25460 

.  74540 

3.9277 

.26328 

3.7983 

1.0341 

.03295 

.96705 

15 

15 

0 

.  25882 

.74118 

3.8637 

.26795 

3.7320 

1  .  0353 

.03407 

.96593 

75 

0 

Co-sine. 

Ver.Sin. 

Secant. 

Co-tan. 

Tang. 

Co-sec. 

Co-vers. 

Sine. 

0 

M 

From  75°  to  90°  read  from  bottom  of  table  upwards. 


AND    CONDENSERS 


FOR   EVERV  SERVICE 


421 


Natural  Trigonometrical  Functions — Continued 


o 

M. 

Sine. 

Co-vers. 

Co-sec. 

Tang. 

Co-tan. 

Secant. 

Ver.Sin. 

Co-sine 

15 

0 

.25882 

.74118 

3.8637 

.26795 

3  .  7320 

1.0353 

.03407 

.  96593 

75 

0 

15 

.  26303 

.73697 

3.8018 

.27263 

3  .  6680 

1.0365 

.03521 

.96479 

45 

30 

.26724 

.73276 

3  .  7420 

.27732 

3.6059 

1  .  0377 

.03637 

.96363 

30 

45 

.27144 

.72856 

3.6840 

.28203 

3  .  5457 

1  .  0390 

.06574 

.96246 

15 

16 

0 

.27564 

.72436 

3.6280 

.28674 

3.4874 

1.0403 

.03874 

.96126 

74 

0 

15 

.27983 

.72017 

3  .  5736 

.29147 

3.4308 

1.0416 

.03995 

.96005 

45 

30 

.  28402 

.71598 

3  .  5209 

.29621 

3.3759 

1.0429 

.04118 

.95882 

30 

45 

.  28820 

.71180 

3.4699 

.30096 

3.3226 

1  .  0443 

.04243 

.95757 

15 

17 

0 

.29237 

.  70763 

3.4203 

.30573 

3.2709 

1.0457 

.04370 

.95630 

r.\ 

0 

15 

.29654 

.70346 

3.3722 

.31051 

3  .  2205 

1.0471 

.04498 

.95502 

45 

30 

.30070 

.69929 

3  .  3255 

.31530 

3.1716 

1.0485 

.04628 

.95372 

30 

45 

.30486 

.69514 

3.2801 

.32010 

3.1240 

1.0500 

.04760 

.95240 

15 

18 

0 

.30902 

.69908 

3.2361 

.32492 

3.0777 

1.0515 

.04894 

.95106 

72 

c 

15 

.31316 

.68684 

3.1932 

.32975 

3.0326 

1.0530 

.05030 

.94970 

45 

30 

.31730 

.68270 

3.1515 

.33459 

2.9887 

1.0545 

.05168 

.94832 

30 

45 

.32144 

.67856 

3.1110 

.33945 

2.9459 

1.0560 

.05307 

.94693 

15 

19 

0 

.32557 

.67443 

3.0715 

.34433 

2.9042 

1.0576 

.05448 

.  94552 

71 

0 

15 

.  32969 

.67031 

3.0331 

.34921 

2.8636 

1.0592 

.05591 

.94409 

45 

30 

.33381 

.66619 

2.9957 

.35412 

2.8239 

1.0608 

.05736 

.94264 

30 

45 

.33792 

.66208 

2.9593 

.35904 

2.7852 

1.0625 

.05882 

.94118 

15 

2<) 

0 

.34202 

.65798 

2.9238 

.36397 

2.7475 

1.0642 

.06031 

.  93969 

70 

0 

15 

.34612 

.653S8 

2.8S92 

.36892 

2.7106 

1  .  0659 

.06181 

.93819 

45 

30 

.35021 

.64979 

2  .  8554 

.  37388 

2.6746 

1.0676 

.06333 

.93667 

30 

15 

.35429 

.64571 

2  .  8225 

.37887 

2.6395 

1.0694 

.06486 

.93514 

15 

21 

0 

.35837 

.64163 

2  .  7904 

.  38386 

2.6051 

1.0711 

.06642 

.93358 

69 

0 

15 

.36244 

.63756 

2.7591 

.38888 

2.5715 

1.0729 

.06799 

.93201 

4o 

30 

.36650 

.63350 

2.7285 

.39391 

2  .  5386 

1.0748 

.06958 

.93042 

30 

45 

.37056 

.62944 

2.6986 

.39896 

2  .  5065 

1.0766 

.07119 

.92881 

15 

22 

0 

.37461 

.62539 

2.6695 

.40403 

2.4751 

1.0785 

.07282 

.92718 

6» 

0 

15 

.37865 

.62135 

2.6410 

.40911 

2.4443 

1.0804 

.07446 

.92554 

45 

30 

.38268 

.61732 

2.6131 

.41421 

2.4142 

1  .  0824 

.07612 

.92388 

30 

45 

.38679 

.61329 

2  .  5859 

.41933 

2.3847 

1  .  0844 

.07780 

.92220 

15 

23 

0 

.39073 

.60927 

2  .  5593 

.42447 

2.3559 

1.0864 

.07950 

.92050 

67 

0 

15 

.39474 

.60526 

2  .  5333 

.42963 

2.3276 

1.0884 

.08121 

.91879 

45 

30 

.39875 

.60125 

2  .  5078 

.43481 

2.2998 

1.0904 

.08294 

.91706 

30 

45 

.40275 

.  59725 

2.4829 

.44001 

2.2727 

1.0925 

..08469 

.91531 

15 

24 

0 

.40674 

.  59326 

2.4586 

.44523 

2.2460 

1.0946 

.08645 

.91355 

66 

0 

15 

.41072 

.  58928 

2.4348 

.45047 

2.2199 

1.0968 

.08824 

.91176 

45 

30 

.41469 

.58531 

2.4114 

.45573 

2  .  1943 

1.0989 

.09004 

.90996 

30 

45 

.41866 

.58134 

2  .  3886 

.46101 

2.1692 

1.1011 

.09186 

.90814 

15 

25 

0 

.42262 

.57738 

2.3662 

.46631 

2.1445 

1.1034 

.09369 

.90631 

65 

0 

15 

.42657 

.57343 

2.3443 

.47163 

2.1203 

1.1056 

.09554 

.90446 

45 

30 

.43051 

.56^49 

2.3228 

.47697 

2.0965 

1  .  1079 

.09741 

.90259 

33 

45 

.43445 

.56555 

2.3018 

.48234 

2.0732 

1.1102 

.09930 

.90070 

15 

26 

0 

.43837 

.56163 

2.2812 

.48773 

2.0503 

1.1126 

.10121 

.89879 

64 

0 

15 

.44229 

.55771 

2.2610 

.49314 

2.0278 

1.1150 

.10313 

.89687 

45 

30 

.44620 

.  55380 

2.2412 

.49858 

2.0057 

1.1174 

.  10507 

.89493 

30 

45 

.45010 

.  54990 

2.2217 

.  50404 

1.9840 

1.1198 

.  10702 

.89298 

15 

27 

0 

.45399 

.54601 

2.2027 

.50952 

1.9626 

1.1223 

.  10899 

.89101 

63 

0 

15 

.45787 

.54213 

2.1840 

.51503 

1.9416 

1.1248 

.11098 

.  88902 

45 

30 

.46175 

.53825 

2.1657 

.52057 

1.9210 

1.1274 

.11299 

.88701 

30 

45 

.46561 

.53439 

2.1477 

.52612 

1.9007 

1  .  1300 

.11501 

.88499 

15 

28 

0 

.46947 

.53053 

2.1300 

.53171 

1.8807 

1.1326 

.11705 

.  88295 

62 

0 

15 

.47332 

.52668 

2.1127 

.  ft3732 

1.8611 

1.1352 

.11911 

.  88089 

45 

30 

.47716 

.  52284 

2.0957 

.54295 

1.8418 

1.1379 

.12118 

.87882 

. 

30 

45 

.48099 

.51901 

2.0790 

.54862 

1  .  8228 

1  .  1406 

.12327 

.87673 

15 

29 

0 

.48481 

.51519 

2  .  0627 

.55431 

1  .  8040 

1.1433 

.12538 

.87462 

61 

0 

15 

.48862 

.51138 

2.0466 

.56003 

1  .  7856 

1.1461 

.12750 

87250 

45 

30 

.49242 

.50758 

2  .  0308 

.56577 

1.7675 

1.1490 

.12964 

.  87036 

30 

45 

.49622 

.50378 

2.0152 

.57155 

1  .  7496 

1.1518 

.13180 

86820 

15 

30 

0 

.50000 

.50000 

2.0000 

.57735 

1  .  7320 

1.1547 

.13397 

86603 

60 

0 

Co-sine. 

Ver.Sin. 

Secant. 

Co-tan. 

Tang. 

Co-sec. 

Co-vers. 

Sine. 

0 

M 

From  60°  to  75°  read  from  bottom  of  ^able  upwards. 


422 


,  B 

ATTLE 

c 

REE 

K,     1 

MIC 

HIG 

AN, 

U. 

S. 

A. 

-1 

Natural  Trigonometrical  Functions — Continued 


M. 

Sine. 

Co-vers 

Co-sec. 

Tang. 

Co-tan. 

Secant. 

Ver.Sin 

Co-sin 

3   0 

.  50000 

.50000 

2.0000 

.57735 

1.7320 

1.1547 

.13397 

.86603 

6 

0 

15 

.50377 

.49623 

1.9850 

.58318 

1.7147 

1.1576 

.13616 

.86384 

45 

30 

.50754 

.49246 

1.9703 

.58904 

1.6977 

1  .  1606 

.  13837 

.86163 

30 

45 

.51129 

.48871 

1.955S 

.59494 

1  .  6808 

1  .  1636 

.  14059 

.85941 

15 

I   0 

.51504 

.48496 

1.9416 

.60086 

1.6643 

1.1666 

.  14283 

.85717 

5 

0 

15 

.51877 

.48123 

1.9276 

.60681 

1  .  6479 

1.1697 

.  14509 

.85491 

45 

33 

.  52250 

.47750 

1.9139 

.61280 

1.6319 

1  .  1728 

.14736 

.85264 

30 

45 

.52621 

.47379 

1.9004 

.61882 

1.6160 

1.1760 

.  14965 

.  85035 

15 

•  o 

.52992 

.47008 

1.8871 

.62487 

1  .  6003 

1.1792 

.15195 

.  84805 

5 

0 

15 

.53361 

.46639 

1  .  8740 

.63095 

1.5849 

1.1824 

.15427 

.84573 

45 

30 

.53730 

.46270 

1.8612 

.63707 

1.5697 

1.1857 

.15661 

.84339 

30 

45 

.51097 

.45903 

1.8485 

.64322 

1.5547 

1.1890 

.15896 

.84104 

15 

I   0 

.54464 

.45536 

1.8361 

.64941 

1.5399 

1.1924 

.16733 

.83867 

5 

0 

15 

.54829 

.45171 

1  .  8238 

.65563 

1.5253 

1  .  1958 

.16371 

.83629 

45 

30 

.55194 

.44806 

1.8118 

.66188 

1.5108 

1.1992 

.16611 

.  83389 

30 

45 

.55557 

.44443 

1.7999 

.66818 

1.4966 

1  .  2027 

.16853 

.83147 

15 

0 

.55919 

.44081 

1  .  7883 

.67451 

1.4826 

1  .  2062 

.  17096 

.82904 

5< 

0 

15 

.56280 

.43720 

1  .  7768 

.68807 

1.4687 

1  .  2098 

.17341 

.82659 

45 

30 

.56641 

.43359 

1.7655 

.63728 

1.4550 

1.2134 

.  17587 

.82413 

30 

45 

.  57000 

.43000 

1.7544 

.69372 

1.4415 

1.2171 

.17835 

.82165 

15 

0 

.57358 

.42642 

1  .  7434 

.70021 

1.4281 

1  .  2208 

.18085 

.81915 

55 

0 

15 

.57715 

.42285 

1  .  7327 

.  70673 

1.4150 

1.2245 

.18336 

.81664 

45 

30 

.58070 

.41930 

1.7220 

.71329 

1.4019 

1.2283 

.  18588 

.81412 

30 

45 

.  58425 

.41575 

1.7116 

.71990 

1.3891 

1  .  2322 

.18843 

.81157 

15 

0 

.  58779 

.41221 

1.7013 

.  72654 

1.3764 

1.2361 

.  19098 

.80902 

5z 

0 

15 

.59131 

.40869 

1.6912 

.73323 

1.3638 

1  .  2400 

.19356 

.  80644 

45 

30 

.  59482 

.40518 

1.6812 

.  73996 

1.3514 

1  .  2440 

.19614 

.80386 

30 

45 

.  59832 

.40168 

1.6713 

.74673 

1.3392 

1.2480 

.  19875 

.80125 

15 

0 

.60181 

.39819 

1.6616 

.75355 

1  .  3270 

1.2521 

.20136 

.  79864 

tl 

0 

15 

.60529 

.39471 

1.6521 

.76042 

1.3151 

1  .  2563 

.  20400 

.79600 

45 

30 

.  60876 

.39124 

1.6427 

.76733 

1.3032 

1  .  2605 

.,20665 

79335 

30 

45 

.61222 

.38778 

1  .  6334 

.77428 

1.2915 

1.2647 

.20931 

79069 

15 

0 

.61566 

.38434 

1.6243 

.78129 

1  .  2799 

1  .  2690 

.21199 

78801 

52 

0 

15 

.61909 

.38091 

1.6153 

.78834 

1.2685 

1  .  2734 

.21468 

78532 

45 

30 

.62251 

.37749 

1  .  6064 

.  79543 

1.2572 

1.2778 

.21739 

78261 

30 

45 

.62592 

.  37408 

1  .  5976 

.80258 

1.2460 

1.2822 

.22012 

77988 

15 

0 

.  62932 

.37068 

1  .  5890 

.80978 

1.2349 

1  .  2868 

.22285 

77715 

51 

0 

15 

.63271 

.  36729 

1  .  5805 

.81703 

1.2239 

1.2913 

.22561 

77139 

45 

30 

.63603 

.  36392 

1.5721 

.82434 

1.2131 

1.2960 

.22838 

77162 

30 

45 

.63914 

.  36056 

1.5639 

.83169 

1  .  2024 

1  .  3007 

.23116 

76884 

15 

0 

.64279 

.35721 

1.5557 

.83910 

1.1918 

1  .  3054 

.23396 

76604 

50 

0 

15 

.64612 

.  35388 

1  .  5477 

.84656 

1.1812 

1.3102 

.23877 

76323 

45 

30 

.64945 

.35055 

1  .  5398 

.85408 

1.1708 

1.3151 

.  23959 

76041 

30 

45 

.  65276 

.34724 

1.5320 

.86165 

1.1606 

1  .  3200 

.24244 

75756 

15 

0 

.65606 

.3*394 

1  .  5242 

.86929 

1  .  1504 

1  .  3250 

.24529 

75471 

9 

0 

15 

.  65935 

.  34065 

1.5166 

.87698 

1.1403 

1.3301 

.24816 

75184 

45 

30 

.66262 

.33738 

1  .  5092 

.  88172 

1.1303 

1  .  3352 

.25104 

74896 

30 

45 

.66588 

.33412 

1.5018 

.89253 

1.1204 

1  .  3404 

.25394 

74606 

15 

0 

.66913 

.33087 

1.4945 

.90040 

1.1106 

1  .  3456 

.25686 

74314 

18 

0 

15 

.67237 

.32763 

1.4873 

.90834 

1  .  1009 

1  .  3509 

.25978 

74022 

45 

30 

.67559 

.32441 

1.4802 

.91633 

1.0913 

1.3563 

.26272 

73728 

30 

45 

.  67880 

.32120 

1.4732 

.92439 

1.0818 

1.3618 

.26568 

73432 

15 

0 

.68200 

.31800 

1.4663 

.93251 

1  .  0724 

1.3673 

.26865 

73135 

17 

0 

15 

.68518 

.31482 

1.4595 

.94071 

1.0630 

1.3729 

.27163 

72837 

45 

30' 

.  68835 

.31165 

1.4527 

.94896 

1  .  0538 

1  .  3786 

.27463 

72537 

30 

45 

.69151 

.  30849 

1.4461 

.95729 

1  .  0446 

1.3843 

.27764 

72236 

15 

0 

.69466 

.30534 

1.4396 

.96569 

1.0355 

1  .  3902 

.28066 

71934 

16 

0 

15 

.69779 

.30221 

1.4331 

.97416 

1.0265 

1.3961 

.  28370 

71630 

45 

30 

.70091 

'.29909 

1.4267 

.98270 

1.0176 

1  .  4020 

.28675 

71325 

30 

45 

.70401 

.29599 

1  .  4204 

.99131 

1.0088 

1.4081 

.28981 

71019 

15 

0 

.70711 

.  29289 

1.4142 

roooo 

1  .  0000 

1.4142 

.29289 

70711 

15 

0 

Co-sine. 

Ver.  Sin. 

Secant. 

Co-  tan. 

Tang. 

Co-sec. 

Co-vers. 

Sine. 

0 

M. 

Prom  40°  to  60°  read  from  bottom  of  table  upwards: 


423 


Useful    Information — Comparison  of 
Thermometers 


Cent 

Reau. 

Fahr. 

Cent 

Reau 

Fahr. 

Cent. 

Reau 

Fahr. 

—40 

—32.0 

—40.0 

21 

16.8 

69.8 

62 

49.6 

143.6 

—38 

—30.4 

—36.4 

22 

17.6 

71.6 

63 

50.4 

145.4 

—36 

—28.8 

—32.8 

23 

18.4 

73.4 

64 

51.2 

147.2 

—34 

—27.2 

—29.2 

24 

19.2 

75.2 

65 

52.0 

149.0 

—32 

—25.6 

—25.6 

25 

20.0 

77.0 

66 

52.8 

150.8 

—30 

—24.0 

—22.0 

26 

20.8 

78.8 

67 

53  .  6 

152.6 

—28 

—22.4 

—18.4 

27 

21.6 

80.6 

68 

54.4 

154  4 

—26 

—20.8 

—14.8 

28 

22.4 

82.4 

69 

55.2 

156.2 

—24 

—19.2 

—11.2 

29 

23.2 

84.2 

70 

56.0 

158.0 

—22 

—17.6 

—  7.6 

30 

24.0 

86.0 

71 

56.8 

159.8 

—20 

—16.0 

—  4.0 

31 

24.8 

87.8 

72 

57.6 

161.6 

—18 

—14.4 

—  0.4 

32 

25.6 

89.6 

73 

58.4 

163.4 

—16 

—12.8 

+  3.2 

33 

26.4 

91.4 

74 

59  .  2 

165.2 

—14 

—11.2 

6.8 

34 

27.2 

93.2 

75 

60.0 

167.0 

—12 

—  9.6 

10.4 

35 

28.0 

95.0 

76 

60.8 

168.8 

—10 

—  8.0 

14.0 

36 

28.8 

96.8 

77 

61.6 

170.6 

—  8 

—  6.4 

17.6 

37 

29.6 

98.6 

78 

62.4 

172.4 

—  6 

—  4.8 

21.2 

38 

30.4 

100.4 

79 

63.2 

174.2 

—  4 

—  3.2 

24.8 

39 

31.2 

102.2 

80 

61.0 

176.0 

2 

—  1.6 

28.4 

40 

32.0 

104.0 

81 

64.8 

177.8 

6 

0.0 

32.0 

41 

32.8 

105.8 

82 

65.6 

179.6 

+  1 

+  0.8 

33.8 

42 

33.6 

107.6 

83 

66.4 

181.4 

2 

1.6 

35.6 

43 

31.4 

109.4 

84 

67.2 

183.2 

3 

2.4 

37.4 

44 

35.2 

111.2 

85 

68.0 

185.0 

4 

3.2 

39.2 

45 

36.0 

113.0 

86 

68.8 

186.8 

5 

4.0 

41.0 

46 

36.8 

114.8 

87 

69.6 

188.6 

6 

4.8 

42.8 

47 

37.6 

116.6 

88 

70.4 

190.4 

7 

5.6 

44.6 

48 

38.4 

118.4 

89 

71.2 

192.2 

8 

6.4 

46.4 

49 

39.2 

120.2 

90 

72.0 

194.0 

9 

7.2 

48.2 

50 

40.0 

122.0 

91 

72.8 

195.8 

10 

8.0 

50.0 

51 

40.8 

123.8 

92 

73.6 

197.6 

11 

8.8 

51.8 

52 

41.6 

125.6 

93 

74.4 

199.4 

12 

9.6 

53.6 

53 

42.4 

127.4 

94 

75.2 

201.2 

13 

10.4 

55.5 

54 

43.2 

129.2 

95 

76.0 

203.0 

14 

11.2 

57.2 

55 

44.0 

131.0 

96 

76.8 

204.8 

15 

12.0 

59.0 

56 

44  8 

132.8 

97 

77.6 

206.6 

16 

12.8 

60.8 

57 

45.6 

134.6 

98 

78.4 

208.4 

17 

13.6 

62.6 

58 

46.4 

136.4 

99 

79.2 

210.2 

18 

'14.4 

64.4 

59 

47.2 

138.2 

100 

80.0 

212.0 

19 

15.2 

66.2 

60 

48.0 

140  0 

20 

16.0 

68.0 

61 

48.8 

141.8 

Freezing  point  on  Fahrenheit  scale  is  +  32  degrees:  boiling  point,  212  degrees. 

Freezing  point  on  Centigrade  scale  is  +  0  degrees;  boiling«point,  100  degrees. 

Freezing  point  on  Reaumur  scale  is+0  degrees;  boiling  point,  80  degrees. 

Of  water  at  sea  level  at  normal  barometer  pressure  (29.9  inch). 

The  "absolute  zero"  of  temperature  denotes  that  condition  of  matter  at  whirh  heat 
ceases  to  exist.  At  this  point  a  body  would  be  wholly  deprived  of  heat  and  a  gas  would  exert 
no  pressure. 

The  absolute  zero  on  the  Fahrenheit  scale  is  about  461  degrees  below  zero. 

The  absolute  zero  on  the  Centigrade  scale  is  about  274  degrees  below  zero. 

The  absolute  zero  on  the  Reaumur  scale  is  about  219  degrees  below  7ero. 

An  English  unit  of  heat  (B.  T.  U.)  is  the  quantity  required  to  raise  one  pound  of  water 
one  degree  Fahrenheit.  A  metric  unit  of  heat  or  metric  caloric  (M.  C.)  is  the  quantity 
of  heat  required  to  raise  one  litre  of  water  one  degree  Centigrade. 


PUMPING    MACHINERY,    AIR   COMPRESSOR 


424 


r     BATTLE      CREEK.     MICHIGAN.     U.  S._A"_J 

Table  of  Decimal  Equivalents  of  8ths,  16ths, 
32nds,  and  64ths  of  an  Inch 

8ths 

A   =    -28125 

if   =    .296875 

y%  =  .125 

H   =    .34375 

|}   =    .328125 

M   =    -250 

if   =    .40625 

If   =    .359375 

ys  =  .375 

if    =    .46875 

If   =    .390625 

'y2  =  .500 

if   =    .53125 

H   =    .421875 

5/s   =    .625 

if   =    .59375 

If   =    .453125 

H   =    -750 

U   =    .65625 

li   =    .484375 

7A   =    .875 

|f    =    .71875 

If    =    .515625 

16ths 

|f   =    .78125 

Jf    =    .546875 

TV   =    .0625 
A-   =    .1875 
A   =    .3125 
iV   =    -4375 
A   =    .5625 

|f   =    .84375 
|f   =    .90625 
ff   =    .96875 

64ths 

A   =    .015625 

§1   -    .578125 
ff   =    .609375 
H   =    .640625 
if   =    .671875 
ff   =    .703125 
H   =    .734375 

U   =    .6875 
if   =    .8125 

A   =    .046875 
A   =    -078125 

Jf   =    .765625 
|i   =    .796875 

if   =    .9375 

A   =    -109375 

If   =    .828125 

32nds 

A   =    .140625 

If   =    .859375 

A   =    .03125 

il   =    .171875 

%l   =    .890625 

A   =    .09375 

if   =    .203125 

|J   =    .921875 

A   =    .15625 

if   =    .234375 

11   =    .953125 

A   =    -21875 

H   =    .265625 

|f   =    .984375 

|        AND    CONDENSERS    FOR   EVERY  SERVICE         | 

425 


UNION       STEAM       PUMP 


Decimal  Equivalents  of  Millimeters 
and  Fractions  of  Millimeters 

TU  mm.  =.0003937" 


mm. 

Inches 

mm 

Inches 

mm. 

Inches 

mm. 

Inches 

A 

— 

.00079 

ft 

= 

.03071 

27 

_ 

1  .  06299 

64 



2.51968 

A 

= 

00157 

40 
f  0 

= 

.03150 

28 

= 

1.10236 

65 

— 

2.55905 

& 

•:= 

.00236 

II 

= 

.03228 

29 

= 

1.14173 

66 

— 

2  .  59842 

A 

= 

.00315 

42 
10~ 

= 

.03307 

43 
BO 

= 

.03386 

30 

SB 

1.18110 

67 

= 

2.63779 

& 

= 

.  00394 

44 
10 

= 

.03465 

31 

-- 

1  .  22047 

68 

_ 

2.67716 

tip 

= 

.00472 

32 

= 

1.25984 

69 

= 

2.71653 

& 

sss 

.00551 

45 
10 

= 

.  03543 

33 

= 

1.29921 

70 

_ 

2.75590 

A 

= 

.00630 

BB 

.03622 

34 

is 

1.33858 

71 

_ 

2.79527 

690 

= 

.00709 

4? 

= 

.03701 

5$ 

= 

.03780 

35 

= 

1.37795 

72 

_ 

2  .  83464 

u 

= 

.00787 

11 

10 

= 

.03858 

36 

= 

1.41732 

73 

— 

2.87401 

il 

= 

.00866 

37 

= 

1.45669 

74 

— 

2.91338 

M 

= 

.00945 

1 

= 

.03937 

38 

-3 

1  .  49606 

75 

= 

2.95275 

li 

= 

.01024 

2 

= 

.0787t 

39 

= 

.1.53543 

76 

= 

2.99212 

3 

= 

.11811 

Si 

= 

.01102 

4 

= 

.15748 

40 

= 

1.57480 

77 

= 

3.03149 

43 

= 

.01181 

41 

= 

1.61417 

78 

_ 

3.07086 

43 

•• 

.01260 

5 

= 

.  19685 

42 

-_ 

1.65354 

79 

_ 

3.11023 

45 

= 

.01339 

6 

= 

.23622 

43 

= 

1.69291 

80 

_• 

3.14960 

43 

*" 

.01417 

7 

= 

.27559 

44 

= 

1.73228 

81 

_ 

3.18897 

43 

= 

.01496 

8 

= 

.31496 

9 

= 

.35433 

45 

— 

1.77165 

82 

_ 

3.22834 

§8 

= 

.01575 

46 

= 

1.81102 

83 

= 

3.26771 

u 

= 

.01654 

10 

= 

.39370 

47 

= 

1  85039 

84 

_ 

3.30708 

13 

— 

.01732 

11 

= 

.43307 

48 

= 

1.88976 

85 

M 

3.34645 

ia 

= 

.01811 

12 

_ 

.47244 

49 

= 

1.92913 

86 

_ 

3.38582 

1$ 

= 

.01890 

13 

= 

.51181 

tiS 

01969 

14 

= 

.55118 

50 

= 

1.96850 

87 

= 

3.42519 

§0 

.  \J  JL  J\9s 

07047 

51 

= 

2.00787 

88 

= 

3.46456 

U 

.  \JZ.\Ji*T  1 

071  9fi 

15- 

= 

.  59055 

52 

= 

2.04724 

89 

==: 

3.50393 

IS 

.  \)L  1  —  U 

noonc 

16 

= 

.62992 

53 

= 

2.08661 

90 

= 

3.54330 

§0 

.  uz  zuo 
097R1 

17 

= 

.66929 

54 

== 

2.12598 

91 

ca 

3.58267 

.    UZZOO 

18 

ea 

.  70866 

II 

_ 

.02362 

19 

= 

.74803 

55 

= 

2.16535 

92 

= 

3.62204 

u 

= 

.02441 

56 

= 

2.20472 

93 

— 

3.66141 

u 

_ 

.02520 

20 

= 

.  78740 

57 

= 

2.24409 

94 

= 

3.70078 

u 

_ 

.02598 

21 

= 

.82677 

58 

= 

2.28346 

95 

= 

3.74015 

12 

__ 

.02677 

22 

as 

.86614 

59 

= 

2.32283 

96 

= 

3.77952 

23 

S3 

.90551 

M 

= 

.02756 

24 

±s 

.94488 

60 

= 

2.36220 

97 

= 

3.81889 

18 

= 

.02835 

61 

= 

2.40157 

98 

— 

3.85826 

U 

= 

.02913 

25 

= 

.98425 

62 

= 

2.44094 

99 

IB 

3.89763 

II 

~ 

.02992 

26 

= 

1.02362 

63 

= 

2.48031 

100 

= 

3.93700 

10  mm.  =  1  Centimeter  =  0.393 7  inches. 
10  cm.  =  1  Decimeter  =  3. 93 7  inches. 
10  dm.  =  l  Meter  =  39. 37  Inches. 
25.4  mm.  =  1  English  Inch. 


1 


PUMPING  MACHINERY; 


426 


Circumferences  and  Areas  of  Circles 

Advancing  by  Eighths 


Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

1X 

.04909 

00019 

25/s 

8.2467 

5.4119 

6f4 

21.206 

35.785 

Vo2 

.09818 

.00077 

-211/16 

8.4430 

5.6727 

6% 

21.598 

37.122 

.  14726 

.00173 

2M 

8.6394 

5.9396 

.  19635 

.00307 

213/16 

8.8357 

6.2126 

7 

21.991 

38  .  485 

29452 

.00690 

9.0321 

6.4918 

7y& 

22  .  384 

39.871 

y 

.39270 

.01227 

215/16 

9  .  2284 

6.7771 

734 

22  .  776 

41.282 

s/ 

49087 

.01917 

7% 

23.169 

42.718 

3/1K 

.  58905 

.02761 

3 

9.4248 

7.0686 

7y% 

23  .  562 

44.179 

%2 

.68722 

.03758 

31/16 

9.6211 

7.3662 

75A 

23.955 

45.664 

9.8175 

7  .  6699 

7% 

24  .  347 

47.173 

34 

.78540 

.04909 

33/l6 

10.014 

7.9798 

7H 

24  .  740 

48.707 

%2 

.88357 

.06213 

334 

10.210 

8.2958 

5/1.6 

.98175 

.07670 

35/16 

10.407 

8.6179 

8 

25.133 

50.265 

11/32 

1.0799 

.09281 

3% 

10.603 

8.9462 

83^ 

25  .  525 

51  .  849 

1.1781 

.11045 

37/16 

10  .  799 

9  .  2806 

834 

25.918 

53  .  456 

13i?2 

1  .  2763 

.  12962 

33^ 

10.996 

9.6211 

8% 

26.311 

55.088 

7/ 

1  .  3744 

.15033 

39/16 

11.192 

1  9.9678 

O  I/ 

26  .  704 

56  .  745 

15'32 

1  .  4726 

.17257 

11.388 

10.321 

8% 

27.096 

58  .  426 

x 

3H!6 

11.585 

10.680 

o  a/ 

27  .  489 

60.132 

H 

1  .  5708 

.  19635 

11.781 

11.045 

8JA 

27.882 

61.862 

I?/™ 

1  .  6690 

.22166 

313/16 

11.977 

11.416 

Q/ 

Vl6 

1.7671 

.24850 

12.174 

11.793 

9 

28.274 

63.617 

19/32 

1  .  8653 

.27688 

315/16 

12  .  370 

12.177 

9/^ 

28.667 

65  .  397 

1.9635 

.30680 

934 

29.060 

67.201 

^3 

2.0617 
2.1598 

.33824 
.37122 

4 

12.566 
12  763 

12.566 
12.962 

9^1 

29.452 
29.845 

69  .  029 
70  .  882 

23/32 

2.2580 

.40574 

43C 

12^959 
13.155 

13^364 
13.772 

1% 

30  .  238 
30.631 

72  .  760 
74  .  662 

/€ 

2  .  3562 

.44179 

434 

13.352 

14.186 

9% 

31.023 

76  .  589 

13/f8 

2.4544 
2.5525 

.47937 
.51849 

45/16 
4% 

13.548 
13.744 

14  .  607 
15.033 

10 

31.416 

78  .  540 

2%2 
7/8 

2.6507 
2  .  7489 

.55914 
.60132 

47/l6 

43^ 

13.941 
14.137 

15.466 
15.904 

1031 

31  .809 
32.201 

80.516 
82.516 

2%2 

15/16 

2.8471 
2.9452 

.64504 
.69029 

49/16 

14.334 
14.530 

16.349 
16  .  800 

Wy2 

32  .594 
32.987 

84.541 
86  .  590 

3V32 

3.0434 

.  73708 

411/16 

14.726 
14.923 

17.257 
17.721 

io|| 

33.379 
33  .  772 

88  .  664 
90  .  763 

3   1416 

.7854 

41%  6 

15'll9 

18!  190 

10J- 

34  .  165 

92  .  886 

lVl6 

IH 

3^3379 
3.5343 

!8866 
.9940 

4ifl6 

15.315 
15.512 

18.665 
19.147 

11 

34  .  558 
34  .  950 

95  .  033 
97  .  205 

13/16 

3  .  7306 

1  .  1075 

1  1  IX 

35  343 

99.402 

3.9270 

1.2272 

5 

15.708 

19.635 

110 

35^736 

101  !  62 

15/16 

4.1233 

1  .  3530 

5Vl6 

15.904 

20.129 

1  1  1/ 

36   128 

103.87 

IH 

4.3197 

1.4849 

sys 

16.101 

20  .  629 

11  0 

36^521 

106.  14 

17/16 

1^ 

4.5160 

4.7124 

1.6230 
1.7671 

53/16 

534 

16.297 
16.493 

21.135 
21.648 

11% 

36.914 
37  .  306 

108.43 
110.75 

19/16 

4.9087 

1.9175 

55/16 

16.690 

22.166 

/8 

5.1051 

2.0739 

16.886 

22.691 

12 

37.699 

113.10 

ll6 

5.3014 
5.4978 

2.2365 
2.4053 

5?6 

17  '.082 
17.279 

23.221 

23  .  758 

123^ 

1234 

38.092 
38  .  485 

115.47 
117.86 

113/  g 

5.6941 

2  .  5802 

5^6 

17.475 

24.301 

38  .  877 

120.28 

17A 

5  .  8905 

2.7612 

5% 

17.671 

24.850 

123J 

39  '.  270 

122  '72 

115/16 

6.0868 

2.9483 

5H/16 

17.686 

25.406 

12^6 

39  .  663 

125.19 

5  iM- 

18.064 

25.967 

40  .  055 

127.68 

2 

6.2832 
6.4795 

3.1416 
3.3410 

51%  6 

18.261 
18.457 

26.535 
27.109 

12H 

40  .  448 

130.19 

2%6 

6.6759 

3  .  5466 

515/le 

18.653 

•  27.688 

13 

40.841 

132.73 

23/16 

6.8722 

3.7583 

13H 

41.233 

135.30 

234 

7.0686 

3.9761 

6 

18  .  850 

28  .  274 

1334 

41.626 

137.89 

7.2649 

4  .  2000 

6% 

19.242 

29  .  465 

13% 

42.019 

140.50 

2% 

7.4613 

4.4301 

6^ 

19.635 

30  .  680 

133^ 

42.412 

143.14 

27/16 

7.6576 

4  .  6664 

20  .  028 

31.919 

13% 

42  .  804 

145  .  80 

7.8540 

4.9087 

G\4 

20  .  420 

33.183 

43.197 

148.49 

2%6 

8  .  0503 

5.1572 

6% 

20.813 

34.472 

13J>8 

43.590 

151.29 

AND    CONDENSERS T  FOR    EVERY  SERVICE 


Circumferences  and  Areas  of  Circles— Continued 


Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

14 

14% 

43.982 
44.375 

153.94 
156  .  70 

21% 
21% 

67.152 
67  .  544 

358.84 
363.05 

28% 
,28% 

90.321 
90.713 

649.18 
654  .  84 

14% 

44  .  768 

159.48 

21% 

67  .  937 

367  .  28 

45.160 

162.30 

21% 

68  .  330 

371.54 

29 

91   106 

660  52 

14% 

45  .  553 

165.13 

21% 

68.722 

375.83 

29% 

91^499 

666^23 

14% 

45.946 

167.99 

29% 

91  .892 

671  96 

14% 

46  .  338 

170.87 

22 

69.115 

380.13 

29% 

92  284 

677^71 

14% 

46.731 

173.78 

22% 

69  .  508 

384.46 

29% 

92.677 

683.49 

22% 

69  .  900 

388  .  82 

29% 

93.070 

689  .  30 

15 

47.124 

176.71 

22% 

70  .  293 

393  .  20 

29% 

93.462 

695.  13 

15% 

47.517 

179  .  67 

22% 

70  .  686 

397.61 

29% 

93  .  855 

700  '.  98 

15% 

47.909 

182.65 

22% 

71.079 

402  .  04 

15%  ' 
15% 

48.302 
48  .  695 

185.66 
188  .  69 

22% 
22% 

71.471 
71.864 

406  .  49 
410.97 

30 

30% 

94  .  248 
94  .  640 

706  .  86 
712  70 

15% 

49.087 

191.75 

30% 

95  033 

71  o  '  en 

49  .  480 

49.873 

194.83 
197.93 

23 

23% 
23% 

72.257 
72  .  649 
73  .  042 

415.48 
420  .  00 
424  .  56 

30  % 
30% 
on  5% 

95^426 
95.819 
96   211 

<  i  o  .  oy 
724  .  64 
730  .  62 
7S6  fi^ 

16 

16% 

50.265 
50  .  658 
51.051 

201.06 
204  .  22 
207  .  39 

23% 
231A 
23% 

73.435 
73  .  827 
74  .  220 

429  .  13 
433  .  74 
438  .  36 

OU/g 

30% 
30% 

96  '.  604 
96.997 

742  '.  64 
748.69 

16% 

16% 

17 
17% 
17% 

51.444 
51.836 
52  .  229 
52  .  622 
53.014 

53.407 
53  .  800 
54  .  192 

210.60 
213.82 
217.08 
220  .  35 
223  .  65 

226  .  98 
230  .  33 
233.71 

23% 
23% 

24 

24% 
24% 
24% 
24% 
24% 

74.613 
75.006 

75.398 
75.791 
76  .  184 
76  .  576 
76.969 
77.362 

443.01 
447.69 

452.39 
457.11 
461.86 
466  .  64 
471.44 
476  .  26 

31 
31% 
31% 
31% 
31% 
31% 
31% 
31% 

97.389 
97.782 
98.175 
98.567 
98.960 
99  .  353 
99.746 
100.138 

754  .  77 
760  .  87 
766.99 
773.14 
779.31 
785.51 
791.73 
797.98 

54  .  585 

237.10 

24% 

77  .  754 

481.11 

17% 

54.978 

240  .  53 

24% 

78.147 

485.98 

32 

100.531 

804  .  25 

17% 

55  371 

243  98 

32% 

100  .  924 

810.51 

17% 

55;  763 

247^45 

25 

78.540 

490.87 

32% 

101.316 

816.86 

56  .  156 

250.95 

25% 

78.933 

495  .  79 

32% 

101.709 

823.21 

25% 

79  .  325 

500  .  74 

32% 

102.  102 

829  .  58 

18 

56  .  549 

254  .  47 

25% 

79.718 

505.71 

32% 

102.494 

835.  C7 

56.941 

258.02 

25^ 

80.111 

510.71 

32% 

102  .  887 

8i2.39 

18% 

57.334 

261.59 

25% 

80  .  503 

515.72 

32% 

103  .  280 

848.  b3 

18% 

57.727 

265.18 

25% 

80.896 

520.77 

58.119 

268  .  80 

25% 

81  .  289 

525  .  84 

33 

103.673 

855  .  30 

18% 

58.512 

272.45 

33% 

104  .  065 

861.79 

18% 

58.905 

276.12 

26 

81.681 

530.93 

33% 

104  .  458 

868.31 

18% 

59  .  298 

279.81 

26% 

82  .  074 

536  .  05 

33% 

104.851 

874  .  85 

26  M 

82.467 

541.19 

33  H 

105.243 

881.41 

19 

59.690 

283  .  53 

26% 

82  .  860 

546.35 

33% 

105.636 

888  .  00 

19% 

60  .  083 

287.27 

26% 

83.252 

551.55 

33% 

106.029 

894  .  62 

19% 

60  .  476 

291.04 

26% 

83.645 

556  .  76 

33% 

106.421 

901.26 

19% 

60  .  868 

294  .  83 

26% 

84  .  038 

562  .  00 

19  V$ 

61.261 

298  .  65 

26% 

84.430 

567.27 

34 

106.814 

907.92 

19% 

61.654 

302  .  49 

34% 

107.207 

914.61 

19% 

62.046 

306.35 

27 

84.823 

572.56 

34% 

107.600 

921.32 

19% 

62.439 

310.24 

27% 

85.216 

577.87 

34% 

107.992 

928.06 

27% 

85.608 

583.21 

34% 

108.385 

934.82 

20 

62.832 

314.16 

27% 

86.001 

588  .  57 

34% 

108.778 

941.61 

20% 

63  .  225 

318.10 

27% 

86.394 

593  .  96 

34% 

109.170 

948.42 

20% 

63.617 

322.06 

27% 

86  .  786 

599  .  37 

34% 

109.563 

955.25 

20% 

64.010 

326.05 

27%    • 

87.179 

604.81 

20% 

64  .  403 

330  .  06 

27% 

87.572 

610.27 

35 

109  .  956 

962.11 

20% 

64.795 

334  .  10 

35% 

110.348 

969  .  00 

20% 

65.188 

338.16 

28 

87.965 

615.75 

35% 

110.741 

975.91 

20% 

65.581 

342.25 

28% 

88.357 

621.26 

35% 

111.  134 

982  .  84 

28% 

88.750 

626  .  80 

35% 

111.527 

989  .  80 

21 

65.973 

346  .  36 

28% 

89.143 

632  .  36 

35% 

111.919 

996.87 

21% 

66  .  366 

350.50 

28% 

89  .  535 

637.94 

35% 

112.312 

1003  .  8 

21% 

66  .  759 

354.66 

28% 

89.928 

643.55 

35% 

112.705 

1010.8 

428 


C  REEK. 

MICHIGAN, 

U. 

3:X=I 

Circumferences  and  Areas  of  Circles — Continued 


Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

36 

36% 

113.097 
113.490 

1017.9 
1025.0 

43% 

135.874 
136.267 

1469  .  1 
1477.6 

sou 

50% 

158.650 
159.043 

2003.0 
2012.9 

36  1^ 

113.883 

1032.1 

136.659 

1486.2 

50% 

159.436 

2022.8 

36% 

114.275 

1039.2 

43% 

137.052 

1494.7 

50% 

159.829 

2032  .  8 

36  y^ 

114.668 

1046.3 

43% 

137.445 

1503.3 

36% 

115.061 

1053.5 

43% 

137.837 

1511.9 

51 

160.221 

2042.8 

36% 

115.454 

1060  .  7 

51% 

160.614 

2052  .  8 

36% 

115.846 

1068.0 

44 

138.230 

1520.5 

51% 

161.007 

2062.9 

44% 

138.623 

1529.2 

51% 

161.399 

2073  .  0 

37 

116.239 

1075.2 

44% 

139.015 

1537.9 

161.792 

2083  .  1 

116.632 

1082.5 

44% 

139  .  408 

1546.6 

51% 

162.185 

2093  .  2 

37  jj 

117.024 

1089.8 

44^ 

139.801 

1555.3 

51% 

162.577 

2103  3 

37% 

117.417 

1097.1 

44% 

140.194 

1564.0 

51% 

162.970 

2113.5 

371-4 

117.810 

1104.5 

44% 

140  .  586 

1572.8 

37% 

118.202 

1111.8 

44% 

140.979 

1581.6 

52 

163  .  363 

2123.7 

37% 

118.596 

1119.2 

52% 

163.756 

2133.9 

37% 

118.988 

1126.7 

45 

141.372 

1590.4 

52% 

164.148 

2144.2 

45% 

141.764 

1599.3 

52% 

164.541 

2154.5 

38 

119.381 

1134.1 

45% 

142.157 

1608  .  2 

52% 

164.934 

2164.8 

38% 

119.773 

1141.0 

45% 

142.550 

1617.0 

52% 

165  .  326 

2175.1 

38  14 

120.166 

1149.1 

45  ^ 

142.942 

1626.0 

52% 

165.719 

2185.4 

38% 

120.559 

1156.6 

45% 

143  .  335 

1631.9 

52,% 

166.112 

2195.8 

38^ 

120.951 

1164.2 

45% 

143  .  728 

1643.9 

38% 

121.344 

1171.7 

45% 

144.121 

1652.9 

53 

166.504 

2206  .  2 

38% 

121.737 

1179.3 

53% 

166.897 

2216.6 

38% 

122.129 

1186.9 

46 

144.513 

1661.9 

53% 

167.290 

2227.0 

46% 

144.906 

1670.9 

55% 

167.683 

2237.5 

39 

122.522 

1194.6 

46% 

145.299 

1680.0 

53  1A 

168.075  . 

2248.0 

39  Vs 

122.915 

1202.3 

46% 

145.691 

1689.1 

53% 

168.468 

2258.5 

3914 

123.308 

1210.0 

46  K 

146.084 

1698.2 

53% 

168.861 

2269  .  1 

39% 

123.700 

1217.7 

46% 

146.477 

1707.4 

53% 

169.253 

2279.6 

39  H 

124.093 

1225.4 

46% 

146.869 

1716.5 

39% 

124.486 

1233.2 

46% 

147.262 

1725.7 

54 

169.646 

2290.2 

39% 

124.878 

1241.0 

54% 

170.039 

2300  .  8 

39% 

125.271 

1248.8 

47 

147.655 

1734.9 

170.431 

2311.5 

47% 

148.048 

1744.2 

54% 

170  .  824 

2322  .  1 

40 

125.664 

1256.6 

47% 

148.440 

1753.5 

54  H 

171.217 

2332.8 

40% 

126.056 

1264.5 

47% 

148  .  338 

1762.7 

54% 

171.609 

2343.5 

40% 

126.449 

1272.4 

4  7  IX 

149.226 

1772.1 

54% 

172.002 

2354.3 

40% 

126.842 

1280.3 

47% 

149.618 

1781.4 

54% 

172.395 

2365.0 

40  V6 

127.235 

1288.2 

47% 

150.011 

1790.8 

40% 

127.627 

1296.2 

47.% 

150.404 

1800  .  1 

55 

172.788 

2375  .  8 

40% 

128.020 

1304.2 

55% 

173.180 

2386  .  6 

40% 

128.413 

1312.2 

48 

150.796 

1809  .  6 

55% 

173.573 

2397.5 

48% 

151  .  189 

1819.0 

55% 

173.966 

2408  .  3 

41 

128.805 

1320.3 

48% 

151.582 

1828.5 

55% 

174.358 

2419.2 

41% 

129.198 

1328.3 

48% 

151  .975 

1837.9 

55% 

174.751 

2430.1 

41  % 

129.591 

1336.4 

481/6 

152.367 

18i7.5 

55% 

175.144 

2441.1 

4  1  % 

129.983 

1344.5 

48% 

152.760 

1857.0 

55% 

175.536 

2452.0 

41  H 

130.376 

1352.7 

153.153 

1866.5 

41% 

1  30  .  769 

1360.8 

48% 

153.545 

1876  .  1 

56 

175.929 

2463.0 

41% 

131.161 

1369.0 

56% 

176.322 

2474.0 

"1% 

131.554 

1377.2 

49 

153.938 

1885.7 

56% 

176.715 

2485.0 

49% 

154.331 

1895.4 

56% 

177.107 

2496.1 

42 

131.947 

1385.4 

49% 

154  .  723 

1905.0 

56  U 

177.500 

2507.2 

42% 

132.340 

1393.7 

49% 

155.116 

1914.7 

56% 

177.893 

2518.3 

42  jl 

132.732 

1402.0 

49% 

155.509 

1924.4 

56% 

178.285 

2529.4 

42% 

133.125 

1410.3 

49% 

155.902 

1934.2 

56% 

178.678 

2540.6 

133.518 

1418.6 

49% 

156.294 

1943.9 

42% 

133.910 

1427.0 

49% 

156.687 

1953.7 

57 

179.071 

2551.8 

42% 

134.303 

1435.4 

57% 

179.463 

2563.0 

42% 

134  .  696 

1443  .  8 

50 

157.080 

1963.5 

179.856 

2574.2 

50% 

157.472 

1973.3 

57% 

180.249 

2585.4 

43 

135.088 

1452.2 

50% 

157.865 

1983.2 

57^ 

180.642 

2596  .  7 

43% 

135.481 

1460.7 

50% 

158.258 

1993.1 

57% 

181.034 

2608.0 

429 


Circumferences  and  Areas  of  Circles— Continued 


Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

573/ 

181.427 

2619.4 

65 

204  .  204 

3318.3 

72% 

226  .  980 

4099  .-8 

57% 

181.820 

2630.7 

65% 

204  .  596 

3331.1 

72% 

227.373 

4114.0 

65!^ 

204  .  989 

3343.9 

72% 

227.765 

4128.2 

58 

182.212 

2642.1 

65% 

205  .  382 

3356  .  7 

72% 

228.158 

4142.5 

58% 

182.605 

2653  .  5 

65% 

205.774 

3369.6 

72% 

228.551 

4156.8 

58% 

182.998 

2654.9 

65% 

206.167 

3382.4 

72% 

228.994 

4171.1 

58% 

183  .  390 

2676.4 

65% 

206  .  560 

3395.3 

58% 

183.783 

2687.8 

65% 

206.952 

3408.2 

73 

229.336 

4185.4 

58% 

184.176 

2699  .  3 

73% 

229  .  729 

4199.7 

58% 

184  .  569 

2710.9 

66 

207.345 

3421.2 

73% 

230.122 

4214.1 

58% 

184.961 

2722.4 

66% 

207.738 

3434.2 

73% 

230.514 

4228.5 

66% 

208.131 

3447.2 

73% 

230.907 

4242.9 

59 

185.354 

2734.0 

66% 

208.523 

3460.2 

73% 

231  .300 

4257.4 

59% 

185.747 

2745.6 

66% 

208.916 

3473.2 

73% 

231.692 

4271.8 

59  X 

186.139 

2757.2 

66% 

209  .  309 

3486.3 

73% 

232.085 

4286.3 

59% 

186.532 

2768.8 

66% 

209.701 

3499  .  4 

59% 

186.925 

2780  .  5 

66% 

210.094 

3512.5 

74 

232.478 

4300  .  8 

59% 

187.317 

2792.2 

74% 

232.871 

4315.4 

59% 

187.710 

2803.9 

67 

210.487 

3525.7 

74% 

233.263 

4329.9 

59% 

188.103 

2815.7 

67% 

210.879 

3538  .  8 

74% 

233  .  656 

4344.5 

67% 

211.272 

3552.0 

234.049 

4359.2 

60 

188.496 

2S27.4 

211.665 

3565.2 

74% 

234.441 

4373.8 

60% 

188.888 

2839  .  2 

67% 

212.058 

3578.5 

234  .  834 

4388.5 

60% 

189.281 

2851.0 

67% 

212.450 

3591.7 

74% 

235.227 

4403.1 

60% 

189.674 

2862.9 

67% 

212.843 

3605.0 

60% 

190.006 

2874.8 

67% 

213.236 

3618.3 

75 

235.619 

4417.9 

60% 

190.459 

2886.6 

75% 

238.012 

4132.6 

60% 

190.852 

2898.6 

68 

213.628 

3631.7 

TRL? 

236.405 

4447.4 

60% 

191.244 

2910.5 

68% 

214.021 

3645  .  0 

75  2 

236  .  798 

4462.2 

68% 

214.414 

3658.4 

75% 

237.190 

4477.0 

61 

191.637 

2922.5 

68% 

214.806 

3671.8 

75% 

237.583 

4491.8 

61% 

192.030 

2934  .  5 

68% 

215.199 

3685.3 

75% 

237.976 

4506.7  . 

192.423 

2946  .  5 

68% 

215.592 

3698.7 

75% 

238.368 

4521.5 

61% 

192.815 

2958.5 

68  34 

125.984 

3712.2 

61% 

193.208 

2970  .  6 

68% 

216.377 

3725.7 

76 

238.761 

4536.5 

61% 

193.601 

2982.7 

7o% 

239.154 

4551.4 

193.993 

2994.8 

69 

216.770 

3739.3 

239.546 

4566  .  4 

61% 

194.386 

3006.9 

69% 

217.103 

3752.8 

76% 

239  .  939 

4581.3 

' 

69% 

217.555 

3766.4 

764 

240.332 

4596.3 

62 

194.779 

3019.1 

69% 

217.948 

3780.0 

76% 

240.725 

4611.4 

62% 

195.171 

2031.3 

69% 

218.  3tl 

3793.7 

76% 

241.117 

4626.4 

195.564 

3043  .  5 

69% 

218.733 

3807.3 

76% 

241.510 

4641.5 

62% 

195.957 

3055  .  7 

68  34 

219.126 

3821.0 

62  V$ 

196.350 

3068.0 

69% 

219.519 

3834.7 

77 

241.903 

4656.6 

62% 

196.742 

3080  .  3 

77% 

242  .  295 

4671.8 

62% 

197.135 

3092.6 

70 

219.911 

3848  .  5 

242  .  688 

4686.9 

62% 

197.528 

3104.9 

70% 

220.304 

3862  .  2 

77% 

243.081 

4702.1 

70% 

220.697 

3876.0 

243.473 

4717.3 

63 

197.920 

3117.2 

70% 

221.090 

3889.8 

77% 

243.868 

4732.5 

63% 

198.313 

3129.6 

70% 

221.482 

3903  .  6 

77% 

244  .  259 

4747.8 

63% 

198.706 

3142.0 

70% 

221.875 

3917.5 

77% 

244.652 

4763.1 

63  % 

199.098 

3154.5 

70% 

222.268 

3931.4 

63% 

199.  191 

3166.9 

70% 

222.660 

3945.3 

78 

245.044 

4778.4 

63% 

199.884 

3179.4 

78% 

245.437 

4793.7 

63  34 

200  .  277 

3191.9 

71 

223.053 

3959.2 

78% 

245.830 

4809.0 

63% 

200.669 

3204.4 

71% 

223.446 

3973.1 

78% 

246.222 

4824.4 

71% 

223  .  838 

3987.1 

78% 

246.615 

4839.8 

64 

201.062 

3217.0 

71% 

224.231 

4001.1 

78% 

247.008 

4855.2 

64% 

201.455 

3229.6 

221.624 

4015.2 

78% 

247.400 

4870.7 

64% 

201.847 

3242.2 

71% 

225.017 

4029.2 

78% 

247.793 

4886.2 

64% 

202  .  240 

3254.8 

71  % 

225.409 

4043.3 

64% 

202  .  633 

3267.5 

71% 

225  .  802 

4057.4 

79 

248.186 

4901.7 

64% 

203  .  025 

3280  .  1 

79% 

248.579 

4917.2 

64% 

203.418 

3292.8 

72 

226.195 

4071.5 

79% 

218.971 

4932.7 

64% 

203.811 

3305  .  6 

72% 

226.587 

4085  .  7 

79% 

249.364 

4948.3 

PUMPING    MACHINERY,    AIR   COMPRESS  ORSj 


430 


jp:   B  ATTLE 

C 

REE 

K. 

M 

ICH 

IG 

AN. 

U. 

S. 

A 

a 

Circumferences  and  Areas  of  Circles — Continued 


Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

Diam. 

Circum. 

Area 

7914 

249.757 

4963.9 

86% 

271.355 

5859.6 

93% 

292  .  954 

6820.5 

79  % 

250.149 

4979.5 

86% 

271.748 

5876  .  5 

93% 

293.346 

6847.8 

79% 

250.542 

4995.2 

86% 

272.140 

5893  .  5 

93% 

293  .  739 

6866.1 

79% 

250  .  935 

5010.9 

86% 

272.533 

5910.6 

93% 

294.132 

6884  .  5 

86% 

272.926 

5927.6 

93% 

294  .  524 

6902.9 

80 

251.327 

5026  .  5 

93% 

294.917 

6921.3 

80% 

251.720 

5042.3 

87 

273.319 

5944.7 

80  >£ 

252.113 

5058  .  0 

87% 

273.711 

5961.8 

94 

295.310 

6939  .  8 

80% 

252  .  506 

5073.8 

87% 

274.104 

5978.9 

94% 

295.702 

6958  .  2 

80% 

252.898 

5089  .  6 

87% 

274.497 

5996.0 

94% 

296.095 

6976.7 

80% 

253.291 

5105.4 

87% 

274  .  889 

6103.2 

94% 

296.488 

6995  .  3 

80% 

253  .  684 

5121.2 

87% 

275.282 

6030.4 

94% 

296.881 

7013.8 

80% 

254.076 

5137.1 

87% 

275.675 

6047.6 

94% 

297.273 

7032.4 

87% 

276.067 

6064  .  9 

94% 

297.666 

7051.0 

81 

254.469 

5153.0 

94% 

298.059 

7069  .  6 

81% 

254  .  862 

5168.9 

88 

276.460 

6082.1 

81M 

255.254 

5184.9 

88% 

276.853 

6099.4 

95 

298.451 

7088.2 

81% 

255.647 

5200  .  8 

88  X 

277.246 

6116.7 

95% 

298.844 

7106.9 

81% 

256  .  040 

5216.8 

88% 

277.638 

6134.1 

95  M 

299  .  237 

7125.6 

81% 

256.433 

5232.8 

88% 

278.031 

6151.4 

95% 

299  .  629 

7144.3 

81  % 

256.825 

5248.9 

88% 

278.424 

6168.8 

95% 

300  .  022 

7163.0 

81% 

257.218 

5264.9 

88% 

278.816 

6186.2 

95% 

300.415 

7181.8 

88% 

279  .  209 

6203.7 

95% 

300.807 

7200.6 

82 

257.611 

5281.0 

95% 

301.200 

7219.4 

82% 

25S.003 

5297.1 

89 

279  .  602 

6221.1 

82  14 

258  .  396 

5313.3 

89% 

279.994 

6238.6 

96 

301.593 

7238.2 

82% 

258  .  789 

5329  .  4 

89  % 

280  .  387 

6256.1 

96% 

301.986 

7257.1 

82  % 

259.181 

5345.6 

89% 

280  .  780 

6273.7 

96% 

302.378 

7276.0 

82% 

259  .  574 

5361.8 

89% 

281.173 

6291.2 

96% 

302.771 

7294.9 

82% 

259.967 

5378.1 

89% 

281.565 

6308.8 

96%' 

303  .  164 

7313.8 

82% 

260  .  359 

5394.3 

89% 

281.958 

6326.4 

96% 

303  .  556 

7332.8 

89% 

282.351 

6344.1 

96% 

303.949 

7351.8 

83 

260.752 

5410.6 

96% 

304  .  342 

7370.8 

83% 

261.145 

5426.9 

90 

282.743 

6361.7 

83M 

261.538 

5443.3 

90% 

283.136 

6379.4 

97 

304  .  734 

7389.8 

83% 

261.930 

5*59.6 

90% 

283.529 

6397.1 

97% 

305.127 

7408.9 

83  '4 

262.323 

5476.0 

90% 

283.921 

6441.9 

97i<£ 

305  .  520 

7428.0 

83% 

262.716 

5492.4 

90H 

284.314 

6432.6 

97% 

305.913 

7447.1 

83% 

263.108 

55C8  8 

90% 

284  .  707 

6450.4 

97% 

306  .  305 

7466  .  2 

83% 

263.501 

5525.3 

90% 

285.100 

6468.2 

97% 

306  .  698 

7485  .  3 

90% 

285.492 

6486.0 

97% 

307.091 

7504  .  5 

84 

263.894 

5541  8 

97% 

307.483 

7523.7 

84% 

264.286 

5558  .  3 

91 

2R5  .  885 

6503  .  9 

84  X 

264  .  679 

5574.8 

91% 

286  .  278 

6521.8 

98 

307  .  876 

7543.0 

84% 

265.072 

5591.4 

91% 

286.670 

6539.7 

98% 

308.269 

7562.2 

84% 

255.465 

5607  .  9 

91% 

287.063 

6557.6 

98  ft 

308.661 

7581.5 

84% 

265.857 

5624.5 

91% 

287  .  456 

6575.5 

98% 

309  .  054 

7600  .  8 

84  % 

266  .  250 

5641.2 

91*1 

287.848 

6593.5 

98  M 

309  .  447 

7620.1 

84% 

266.643 

5657.8 

91% 

288.241 

6611.5 

97% 

309  .  840 

7639.5 

/, 

91% 

288  .  634 

6629.6 

98% 

310.232 

7658.9 

85    /' 

267.035 

5674.5 

98% 

310.625 

7678.3 

85% 

267.428 

5691.2 

92 

289  .  027 

6647.6 

85  M 

267.821 

5707.9 

92% 

289.419 

6665.7 

99 

311.018 

7697.7 

85% 

268.213 

5724.7 

92% 

289.812 

6683  .  8 

99% 

311.410 

7717.1 

85  Ms 

268  .  606 

5741.5 

923/g 

290  .  205 

6701.9 

99% 

311.803 

7736.6 

85% 

268.999 

5758.3 

,92% 

290  .  597 

6720.1 

99% 

312.196 

7756  .  1 

85% 

269  .  392 

5775.1 

92% 

290  .  990 

6738.2 

99% 

312.588 

7775.6 

85% 

269  .  784 

5791.9 

92% 

291.383 

6756.4 

99% 

312.981 

7795.2 

92% 

291.775 

6774.7 

99% 

313.374 

7814.8 

86 

270.177 

580878 

99% 

313.767 

7834.4 

86% 

270.570 

5825.7 

93 

292.168 

6792.9 

86% 

270.962 

5842.6 

93% 

292.561 

6811.2 

100 

314.159 

7854.0 

431 


L 

u 

N 

I  0 

N 

STE 

AM 

P 

UM 

P 

C  O 

M  PANV 

Coefficients  of     Linear    Expansion  at    Tempera- 
tures  between   32°  and   222°  Fahr. 


Material 

For 
1°   Cent. 

For 
1°   Fahr. 

Material 

For 
1°    Cent. 

For 
1°  Fahr. 

Aluminum  —  cast  .  .  . 
Aluminum  —  rolled   . 
Antimony  

.0000222 
.0000207 
.0000110 

.0000123 
.0000115 
.0000061 

Steel  —  untempererl 
Steel  —  tempered.  .  . 
Tin  

.0000108 
.0000126 
.0000207 

.0000060 
.  0000070 
.0000115 

Bismuth         

.0000139 

.0000077 

Zinc  

.0000288 

.0000160 

Brass 

0000189 

.0000105 

Brick—  best  stock. 

0000055 

0000031 

0000171 

0000095 

Fire  Brick 

0000049 

0000097 

Gold      '     " 

.0000153 

.0000085 

Building  i  From. 

.0000072 

0000040 

0000108 

0000060 

Stones  }  To 

0000144 

0000080 

Iron  —  Wrought  .... 
Lead 

.0000117 
.0000281 

.0000065 
.0000158 

Glass  .  ._  
Porcelain 

.0000088 
.0000036 

.00000-19 
0000020 

Nickel  

.0000126 

.0000070 

Roman  Cement  .  .  . 

Platinum  
Silver 

.0000087 
.0000198 

.  0000048 
.0000110 

dry  

Slate 

.0000144 
0000104 

.0000080 
0000058 

Wedgewood  ware  .  . 

.  0000088 

.0000049 

Melting   Points   or   Temperatures   of  Fusion 


Solid 

Cent. 

Fahr. 

Solid 

Cent, 

Fahr. 

Aluminum  ...:.... 
Antimony  
Bismuth 

656 
630 
268 
1030 
920 
320 
1487 
1463 
1084 
1064 
2500 
1220  to   1530 
1050  to    1135 
1500  to    1600 
327 

1214 
1166 
514 
1886 
1688 
608 
2709 
2665 
1983 
1947 
4532 
2228  to   2786 
1922  to  2075 
2732  to   2912 
620 

Magnesium  
Manganese  
Mercury  
Nickel 

750 
1207 
—39.7 
1435 
1546 
1753 
62 
2000 
953 
95 
1475 
1420 
232 
1775 
419 

1382 
2205 
—39.5 
2615 
2815 
3187 
144 
3632 
1747 
203 
2687 
2588 
449 
3227 
786 

Brass  
Bronze 

Palladium  
Platinum 

Cadmium  

Chromium  .               .  . 

Potassium  
Rhodium  
Silver 

Cobalt 

Copper  

Gold 

Sodium  
Steel  —  mild  
Steel  —  hard  
Tin  
Vanadium 

Iridium  

Iron  —  cast,  gray,  .  .  . 
f  ron  —  cast,  white  .  .  . 
Eron  —  wrought  
Lead  

Zinc 

432 


BATTLE      CREEK.     MICHIGAN.      U.  S.  A. 


Mensuration  of  Surfaces  and  Volumes 

Area  of  rectangle  =  length  X  breadth. 

Area  of  triangle  =  base  X  YT.  perpendicular  height. 

Diameter  of  circle  =  radius  X  2. 

Circumference  of  circle  =  diameter  X  3.1416 

Area  of  circle  =  square  of  diameter  X  .7854. 

Area  of  sector  of  circle  =  area  of  circle  X  number  of  degrees  in  arc. 

360 

Area  of  surface  of  cylinder  =  circumference  X  length  +  area  of  two  ends. 
To  find  the  diameter  of  circle  having  given  area:  Divide  the  area  by  .7854,  and 
extract  the  square  root. 
To  find  the  volume  of  a  cylinder:   Multiply  the  area  of _ the  section  in  square 

inches  by  the  length  in  inches  =  the  volume  in  cubic  inches.     Cubic  inches 

divided  by  1728  =  volume  in  cubic  feet. 
Surface  of  a  sphere  =  square  of  diameter  X  3.1416 
Solidity  of  a  sphere  =  cube  of  diameter  X  .5236. 
Side  of  an  inscribed  cube  =  radius  of  a  sphere  X  1.1547. 
Area  of  the  base  of  a  pyramid  or  cone,  whether  round,  square  or  triangular, 

multiplied  by  one-third  of  its  height  =  the  solidity. 
Diam.  X  .8862  =  side  of  an  equal  square. 
Diam.  X  .7071  =  side  of  an  inscribed  square. 
Fadius  X  6.2832  =  circumference. 
Circumference  =  3.5446  X  V  Area  of  circle. 
Diameter  =  1.1283  X  V  Area  of  circle. 
Length  of  arc  =  No.  of  degrees  X  .017453  radius. 
Degrees  in  arc  whose  length  equals  radius  =  57°  2958'. 
Length  of  an  arc  of  1°  =  radius  X  .017543. 
Length  of  an  arc  of  1  Min.  =  radius  X  .0002909. 
Length  of  an  arc  of  1  Sec.  =  radius  X  .0000048. 

=     Proportion  of  circumference  to  diameter  =  3.1415926. 
2      =       9.8696044. 
V          =       1.7724538. 
Log.  =       0.49715. 

I/         =       0.31831. 
1/360         =         .002778. 
360/  *       =  114.59. 


433 


UN  ION       S  T  E  AM       P  U  M  P       COM  P  AN  V 


1 


Mensuration  of  Surfaces  and  Volumes  — Continued 


Lineal  feet . .  .  . 

"     yards.  . 

Square  inches .  . 

feet .  .  . 

yards . . 

Acres 

Cubic  inches .  . 
"     feet... 
Circular  inches 
Cyl.  inches.  .  .  . 
"     feet..... 
Links .  . 


Feet 

Width  in  chains 

183346  circular  inches . 
2200  cylindrical  inches 

Cubic  feet 

"     inches  

U.S.  Gallons.. 


Cubic  feet 

inches  .... 
Cyl.  feet  of  water 
Lbs.  Avoir. .  . 


Cubic  feet  of  water 

inch  of  water 

Cyl.  feet  water ". 

"    inch  of  water 

12  U.  S.  gallons  of  water 

240  U.  S.  gallons  of  water 

1 . 8  cubic  feet  of  water 

35 . 88  cubic  feet  of  water 

Column  of  water,  12  inches  high,  and 

1  inch  in  diameter 

U.  S.  bushel.  . 


.00019 
.0006 
.007 
.111 

.0002067 
4840. 

.00058 
.03704 
.00546 
.0004546 
.02909 
.22 
.66 
1.5 
8. 


7.48 
. 004329 
. 13367 
231. 

.8036 
.000468 
6 

.009 
.00045 
62.5 

.03617 
49.1 
. 02842 


X  .0495 

X         1.2446 
X  2150.42 


Miles 

Square  feet, 
yards 
Acres. 

Square  yards. 
Cubic  feet 

yards 

Square  feet 
Cubic  feet 
"     yards 
Yards 
Feet 
Links 

Acres  per  mile 
1  square  foot 
1  cubic  foot 
ILS.  gallons 

Cubic  feet 
"     inches 

U.  S.  bushel 

«       « 

U.  S.  gallons 
Cwt.  (112) 
Tons  (2240) 
Lbs.  Avoir. 


1  cwt. 
1  ton 
1  cwt. 
1  ton 

.341  Lbs. 
Cubic  yards. 

feet 
Cubic  Inches 


I         PUMPING    MAC HINER.Y,    AIR   COMPRESSORS        J 

aa»gg»iui^oL*iPuaaBBtt»«w*fftfBBi»iiftfgitf»BW»»i»ilnrireB^ 


Comparative  Table  of  the  United  States  and 
Metric  Systems 

Denomination  Equivalent 

One  grain  equals  in  grammes 0 . 0648 

One  pound  avoirdupois  equals  in  kilogrammes 0 . 4536 

One  ton  of  2240  pounds  equals  in  tonnes 1 .0160 

One  ton  of  2000  pounds  equals  in  tonnes 0.9071 

One  inch  equals  in  millimetres 25 .400 

One  foot  equals  in  metres 0 . 3048 

One  mile  equals  in  kilometres 1.6094 

One  square  inch  equals  in  square  millimetres .  .  645 . 2 

One  square  foot  equals  in  square  metres 0 . 09291 

One  acre  equals  in  ares  (100  square  metres) 40.47 

One  square  mile  equals  in  square  kilometres 2 . 590 

One  cubic  inch  equals  in  cubic  centimetres 16.39 

One  cubic  foot  equals  in  cubic  metres 0. 02832 

One  cubic  yard  equals  in  cubic  metres 0 . 7646 

One  quart  dry  measure  equals  in  litres 1.101 

One  quart  liquid  or  wine  measure  equals  in  litres  ...  0 . 9465 

One  foot  pound  equals  in  kilogrammetres 0 . 1383 

One  pound  per  foot  equals  in  kilogrammes  per  metre  1 .488 
One  thousand  pounds  per  square  inch  equals  in  kilo- 
grammes per  square  millimetres 0 . 703 

One  pound  per  square  foot  equals  in  kilogrammes  per 

square  metre 4 . 882 

One  pound  per  cubic  foot  equals  in  kilogrammes  per 

cubic  metre 16 . 02 

One  degree  Fahrenheit  equals  in  degrees  Centigrade.  0.5556 

Comparative  Table  of  the  United  States  and 
Metric  Systems 

Denomination  Equivalent 

One  gramme  equals  in  grains 15 . 433 

Dne  kilogramme  equals  in  pounds  avoirdupois 2 . 2047 

One  tonne  equals  in  tons  of  2240  pounds 0 . 9843 

Dne  tonne  equals  in  tons  of  2000  pounds 1 . 1024 

One  millimetre  equals  in  inches 0 . 0394 

One  metre  equals  in  feet 3 . 2807 

One  kilometre  equals  in  miles 0 . 6213 

One  square  millimetre  equals  in  square  inches 0.00155 


CON^D^N  S JSRS  ^ 

435 


§"     UN 

ION 

STEAM 

P  UM  P 

COMPANY      ^J 

Comparative  Table  of  United  States  and 
Metric  Systems — Continued 


Denomination 

One  square  metre  equals  in  square  feet 

One  are  (100  square  metres)  equals  in  acres 

One  square  kilometre  equals  in  square  miles 

One  cubic  centimetre  equals  in  cubic  inches 

One  cubic  metre  or  stere  equals  in  cubic  feet 

One  cubic  metre  equals  in  cubic  yards : 

One  litre  (one  cubic  decimetre)  equals  in  cubic  inches . 

One  litre  equals  in  quarts,  dry  measure 

One  litre  equals  in  quarts,  liquid  or  wine  measure 

One  kilogrammetre  equals  in  foot  pounds 

One  kilogramme  per  metre  equals  in  pounds  per  foot. . 
One   kilogramme   per   square   millimetre   equals   in 

pounds  per  square  inch 

One  kilogramme  per  square  metre  equals  in  pounds 

per  square  foot 

One  kilogramme  per  cubic  metre  equals  in  pounds 

per  cubic  foot 

One  degree  Centigrade  equals  in  degrees  Fahrenheit. 

Metric  Conversion  Table 


1 

61 


Equivalent 
10.763 
0.02471 
0.3861 
0.0610 
35.3105 
3078 
017 
0.908 
1.0566 
7.2313 
0.6720 

1422. 
0 . 2048 

0.0624 
1.8 


Millimetres  X  .03937  =  inches. 
Millimetres  -f-  25.4  =  inches. 
Centimetres  X  .3937  =  inches. 
Centimetres  -7-2.54  =  inches. 
Metres  X  39.37  =  inches. 
Metres  X  3-281  =  feet. 
Metres  X  1.094  =  yards. 
Kilometres  X  .621  =  miles 
Kilometres  -5-  1.6093  =  miles. 
Kilometres  X  3280.8693  =  feet. 
Sq.  Millimetres  X  .00155  =  sq.  in. 
Sq.  Millimetres  -t-  645.1  =  sq.  in. 
Sq.  Centimetres  X  .155  =  sq.  in. 
Sq.  Centimetres  -j-  6,451  =  sq.  in. 
Sq.  Metres  X  10.764  =  sq.  ft. 
vSq.  Kilometres  X  247.1  =  acres. 
Hectare  X  2.471  =  acres. 
Cu.  Centimetres  -T-  16.383  =  cu.  in. 
Cu.  Centimetres  -5-  3.69  =  fl.  drams. 
Cu.  Centimetres  -f-  29.57  =  fluid  oz. 
Cu.  Metres  X  35.315  =  cu.  ft. 
Cu.  Metres  X  1.308  =  cu.  yds. 
Cu.  Metres  X 264.2=  gals.  (231  cu.  in.) 
Litres  X  61.022  =  cu.  in. 
Litres  X  33.84  =  fluid  oz. 
Litres  X  .2642  =  gals.  (231  cu.  in.) 
Litres  -5-  3.78  =  gals.  (231  cu.  in.) 
Litres  -f-  28.316  =  cu.  ft. 
Hectolitres  X  3.531  =  cu.  ft. 
Hectolitres  X  2.84  =  Bu.  (2150.42 
cu.  in.) 


Hectolitres  X  .131  =  cu.  yds. 
Hectolitres  -f-  26.42  =  gals.  (231  cu.in.) 
Grammes  X  15.432  =  grains. 
Grammes  -f-  981  =  dynes. 
Grammes  (water)  -5-  29.57  =  fluid  oz. 
Grammes  -f-  28.35  =  oz.  avoirdupois 
Grammes  per  cu.  cent,  -f-  27.7  =  Ibs. 

per  cu.  in. 

Joule  X  .7373  =  ft.  Ibs. 
Kilo-grammes  X  2.2046  =  pounds. 
Kilo-grammes  X  35.3  =  oz.  avoirdu- 
pois. 
Kilo-grammes  -J-  907.2  =  tons  (2000 

Ibs.) 
Kilo-grammes  per  sq.  cent.  X  14.223  = 

Ibs.  per  sq.  in. 

Kilo-gram-metres  X  7.233  =  ft.  Ibs. 
Kilo-gr.  per  Metre  X  .672  =  Ibs.  per  ft. 
Kilo-gr.  per  cu.  Metre  X  .062  =  Ibs. 

per  cu.  ft. 
Kilo-gr.  per  Cheval  X  2.235  =  Ibs.  per 

H.  P. 

Kilo- Watts  X  1.34  =  Horsepower 
Watts  -T-  746.  =  Horsepower. 
Watts  X  .7373  =  ft.  pounds  p.  second 
Calorie  X  3.968  =  B.  T.  U. 
Cheval  vapeur  X  .9863  =  Horsepower 
(Centigrade  X  1.8)  +  32=deg.  Fahr. 
Franc  X  .193  =  Dollars 
Gravity  Paris  =  980.94  centimetres 

per  sec. 


436 


c 

B  ATTLE 

CREEK.     MICHIGAN, 

U.  S.  A.     "3 

Calorific  Power,  Carbon  Value,  and  Evaporative 
Power  of  Various  Fuels. 

TOTAL  HEAT  OP  COMBUSTION,  OR  CALORIFIC  POWER  OF 

A  FUEL. — The  calorific  power  of  a  fuel  is  the  number  of  units  of  heat  produced 
by  the  combustion  of  1  pound  weight  of  it.  The  unit  of  heat  is  the  amount 
of  heat  required  to  raise  1  pound  of  water  1°  Fahr. 

CARBON  VALUE  OF  FUEL.— The  carbon  value  of  any  fuel  is  the 
weight  of  carbon  in  pounds  having  the  same  calorific  value  as  1  pound  of  the 
fuel.  Carbon  value  equals  calorific  power  of  fuel  divided  by  calorific  power 
of  carbon. 

THEORETICAL  EVAPORATIVE  POWER  OF  FUEL.— The  theo- 
retical evaporative  power  of  fuel  is  stated  in  pounds  of  water  evaporated  from 
and  at  212°  Fahr.,  and  is  obtained  by  dividing  the  calorific  power  of  the  fuel 
by  966. 

ACTUAL  EVAPORATIVE  POWER  OF  COAL  IN  STEAM  BOILERS. 

From  numerous  experiments  on  steam  boilers,  it  appears  that  the  actual 
evaporative  power  of  coal  varies  from  50  per  cent  to  85  per  cent  of  the  theo- 
retical evaporative  power.  An  average  of  a  considerable  number  of  tests 
gave  the  actual  evaporative  power  equal  to  70  per  cent  of  the  theoretical 
evaporative  power  of  the  coal. 


Combustible 

Calorific 
Power 
in 
British 
Thermal 
Units 

Carbon 
Value 

Evapora- 
tive Power 
in  Lbs.  of 
Water  from 
and  at 
212°  Fahr. 

Carbon  —  burned  to  carbonic  acid  .... 
Carbon  —  burned  to  carbonic  oxide  .  .  . 
Carbonic  oxide  
Marsh  gas  
Olefiant  gas  

14544 
4451 
4325 
23513 
21344 

1.000 
.306 
.297 
1.617 
1  468 

15  .  06 
4.61 
4.48 
24.34 
22  10 

Hydrogen  

62032 

4  265 

64  22 

Hydrogen,  deducting  latent  heat  in 
steam  formed  

53338 

3  667 

55  22 

Sulphur  .  

3996 

275 

4  14 

Straw—  with  16  per  cent  water  
Wood  —  kilrr  dried  
Wood  —  air  dried,   with  20  per  cent 
water  
Peat  —  kiln  dried  
Peat  —  air   dried,    with    20   per   cent 
water  

5200 
8000 

5600 
10000 

6500 

.358 
.550 

.385 

.688 

447 

5.38 

8.28 

5.80 
10.35 

6  73 

Charcoal  from  wood  —  cry 

13000 

894 

13  46 

Charcoal  from  peat  —  dry  
Coal  —  lignite  —  air  dried  .  . 

11600 
11000 

.798 
756 

12.01 
11  39 

ifrom 
to 
average 
{from 
to 
average 
Coke      f    from 

13000 
15700 
14100 
14000 
16200 
15000 
12000 

.894 
1.079 
.969 
.963 
1.114 
1.031 
825 

13.46 
16.25 
14.60 
14.49 
16.77 
15.53 
12  42 

I    to 
Block  fuel  • 

13700 
15000 

.942 
1  031 

14.18 
15  53 

Petroleum  

20000 

1  375 

20  70 

Natural  gas  (Pennsylvania  ^  

26000 

1  788 

26  92 

AND    CONDENSERS    FOR   EVERY"  SERVICE 


437 


Weight  and  Specific  Gravity  of  Metals  (Kent) 


' 

Specific  Gravity 
Range  According 
to  Several 
Authorities 

SpecificGra\ity 
Approximate 
Mean  Value 
Used  in 
Calculation 
of  Weight 

Weight 
per  cubic 
Foot 
Pounds 

Weight 
per  Cubic 
Inch 
Pounds 

Aluminum 

2  56     to     2.71 

2  67 

166.5 

0963 

Antimony 

6  66     to     6.86 

6  76 

421.6 

9439 

Bismuth  
Brass,  copper  and  zinc 
80             20 
70            30 
60            40 
50            50 
Brorzej  copper  95  to  80  j 
onze\tin          5  to  20  / 
Cadmium  
Calcium  

9.74     to     9.90 
7.8       to     8.6 

8.52     to     8.96 

8.6       to     8.7 
1.58 

9.82 

(  8.60 
J  8.40 

}  8.36 
(  8.20 
8  .  853 

8.65 

612.4 

536.3 
523.8 
521.3 
511.4 
552.0 

539.0 

.3544 

.3103 
.3031 
.3017 
.2959 
.3195 

.3121 

Chromium 

5.0 

Cobalt       .... 

8.5       to     8.6 

Gold,  pure  
Copper  .  . 

19.245  to  19.361 
8.69     to     8.92 

19.258 
8.853 

1200.9 
552  0 

.6949 
3195 

T      •     1- 

Indium  
Iron,  cast  

22.38     to  23.0 
6.85     to     7.48 

7.218 

1396.0 
450.0 

.8076 
2604 

Iron,  wrought  
Lead    .  .       .      . 

7.4       to     7.9 
11  07     to  11  44 

7.70 
11  38 

480.0 
709  7 

.2779 
4106 

Manganese  
Magnesium  
f    32° 
Mercury  <     60° 

[212° 
Nickel 

7.0      to     8.0 
1  .  69     to     1  .  75 
13.60     to  13.62 
13.58 
13.37     to  13.38 
8  279  to  8  93 

8.00 
1.75 
13.62 
13.58 
13.38 
8  8 

499.0 
109.0 
849  .  3 
846.8 
834.4 
548  7 

.2887 
.0641 
.4915 
.4000 
.4828 
3175 

Platinum  . 

20  33  to  22  07 

21  5 

1347  0 

7758 

Potassium  
Silver  

0.865 
10  474  to  10  511 

10  505 

655  1 

3791 

Sodium  

0  97 

Steel 

7  69*  to     7  932+ 

7  854 

489  6 

2834 

Tin  . 

7  291  to     7  409 

7  350 

458  3 

2652 

Titanium  .... 

5  3 

Tungsten  

17  0       to  17  6 

Zinc  

6  86  to  7  20 

7  00 

436  5 

2526 

*Hard  and  burned.  fVery  pure  and  soft.  The  specific  gravity  decreases  as 
the  carbon  is  increased.  In  the  first  column  of  figures,  the  lowest  »are  usually 
those  of  cast  metals,  which  are  more  or  less  porous;  the  highest  are  of  metals 
finely  rolled  or  drawn  into  wi-re. 


Proportions    of   Various    Compositions   in 
Common   Use 

(!N  ONE  HUNDRED  PARTS) 

Babbit's  metal Tin  89,  copper  3.7,  antimony  7.3 

Fine  yellow  brass Copper  66,  zinc  34 

Gun  metal,  valves,  etc Copper  90,  tin   10 

White  brass , Copper  10,  zinc,  80,  tin  10 

German  silver Copper  33.3,  zinc  33.4,  nickel  33.3 

Church  bells Copper  80,  zinc  5.6,  tin  10.1,  lead  4.3 

Gongs Copper  81.6,  tin  18.4 

Lathe  bushes Copper  80,  tin  20 

Machinery    bearings Copper    87.5,    tin    12.5 

Muntz  metal Copper  60,  zinc  40 

Sheathing  metal Copper  56,  zinc  44 


438 


Various  Tables  Showing   Weights   of  Materials 

Weight  Per  Bushel  of  Different  Grains,  Etc. 


Barley 48  pounds 

Beans 63  pounds 

Buckwheat 46  pounds 

Blue  Grass  Seed 14  pounds 

Corn 56  pounds 

Corn  Meal 50  pounds 

Clover  Seed 60  pounds 

Dried  Apples 22  pounds 

Dried  Peaches 33  pounds 


Flax  Seed 56  pounds 

Hemp  Seed 48  pounds 

Oats 32  pounds 

Peas 64  pounds 

Rye 56  pounds 

Salt , 80  pounds 

Timothy  Seed 45  pounds 

Wheat 60  pounds 

Potatoes  (heaped) 60  pounds 


Weight  Per  Barrel  of, Different  Articles 

Flour 196  pounds         Fish 200pounds 

Salt 280  pounds         Soap 256  pounds 

Beef 200  pounds        Cement 300  pounds 

Pork 200  pounds    | 

56  pounds  of  butter  equals 1  firkin 

100  pounds  of  meal  or  flour  equals 1  sack 

100  pounds  of  grain  or  flour  equals 1  central 

100  pounds  of  dry  fish  equals I  quintal 

100  pounds  of  nails  equals 1  cask 

Miscellaneous  A  rticles 

One  ton  of  (2240  pounds)  cured  hay  equals 425  cubic  feet 

One  ton  of  hay  in  mow  equals 414.37  cubic  feet,  or  a  cube  of  7>^  ft 

Hay,  as  usually  delivered 5  pounds  per  cubic  foot 

Hay,   well   pressed 8  pounds  per  cubic  foot 

Straw,  loose 3*4  pounds  per  cubic  foot 

Straw,  well  pi'essed 5^  pounds  per  cubic  foot 

One  gallon  of  water  (U.  S.) 8.33  pounds 

One  gallon  of  oil 7V\  pounds 

One  gallon  of  molasses .  .  . 11%  pounds 

One  gallon  of  alcohol 6.9  pounds 

One  gallon  of  spirits  of  turpentine 7.31  pounds 

One  keg  of  powder 25  pounds 

Weights,  in  Pounds,  of  Various  Articles 

As  rated  by  Railway  Companies,  when  their  weights 
cannot  otherwise  be  ascertained 

Ashes,  pot  or  pearl barrel,  450  pounds 

Apples  and  barreled  fruits barrel,  200  pounds 

Apples bushel,  50  pounds 

Barley .bushel,  45  pounds 

Beef,  pork,  bacon ]                f    hhd.,  1000  pounds 

Butter,  tallow,  lard f    per      -j     bbl.,  333  pounds 

Salt  fish  and  meat .  .  . J                [  firkin,  100  pounds 

Bran,  feed,  shipstuffs,   oats bushel,  35  pounds 

Buckwheat bushel,  48  pounds 

Bricks,    common ' each        5  pounds 

Bark cord,  2000  pounds 

Charcoal bushel,  22  pounds 

Colce  and  cake  meal .* bushel,  40  pounds 

Clover    seed bushel,  62  pounds 

Eggs barrel,  200  pounds 

Fish  and  salt  meat per  firkin,  100  pounds 

Flour  and  meal per  bushel,  56  pounds;  barrel,  216  pounds 

Grain  and  seeds,  not  stated bushel,  60  pounds 

Hides,     green each,  85  pounds 

Hides,  dry,  salted    or    Spanish each,  33  pounds 

[ce,    coal,    lime bushel,  80  pounds 

Liquors,  malt   and   distilled barrel,  30  pounds 

439 


Weights,  in   Pounds,  of  Various  Articles- 
Continued 

Liquors per     gallon,       10  pounds 

Lumber — pine,  poplar,  hemlock foot   B.    M.,          4  pounds 

Lumber — oak,  walnut,  cherry,  ash foot,  B.  M.,         5  pounds 

Nails  and  spikes keg,     106  pounds 

Onions,  wheat,  potatoes bushel,       60  pounds 

Oysters per  bushel,    100  pounds;   per   1000,     350  pounds 

Plastering  lath per  1000,     600  pounds 

Rosin,    tar,    turpentine barrel,     300  pounds 

Sand,    gravel,    etc ^ per    cubic    foot,     150  pounds 

Shingles , per    1000,   short  900  pounds,   long,  1400  pounds 

Salt •: bushel       70  pounds 

Stone,  undressed , perch,  4000  pounds 

Stone,     dressed per     cubic     foot,      180  pounds 

Timothy  and  light  grass  seed bushel,       40  pounds 

Wood — hickory cord,  4500  pounds 

Wood— oak cord,  3500  pounds 

WEIGHT  OF  ONE  CUBIC  FOOT  OF  PURE  WATER 

At  32°  F.  (freezing  point) 62 . 418  pounds 

At  39. 1°  F.  (maximum  density) 62 . 425  pounds 

At  62°  F.  (standard  temperature) 62 .  355  pounds 

At  212°  F.  (boiling  point,  under  1  atmosphere) 59 .  76  pounds 

American  gallon  equals  231  cubic  inches  of  water  at  62°  F.  equals 8 . 3356  pounds 

British  gallon  equals  277.274  cubic  inches  of  water  at  62°  F.  equals 10  pounds 


Weight  and  Specific  Gravity  of   Liquids 


Liquids   at   32°   F. 

Weight  of  one 
Cubic  Foot 
Pounds 

Weight  of  one 
Gallon  (Im- 
perial) Pounds 

Specific 
Gravity 
Water  =  1 

Mercury  ... 

848.7 
185.1 
114.9 
96.8 
95.5 
77.4 
76.2 
67.4 
64.3 
64.05 
62.425 
62.9 
61.9 
58.7 
58.1 
57.4 
57.4 
57.1 
54.3 
51.2 
54.9 
53.1 
69.3 
67.4 
55.6 
55.6 
54.3 
44.9 
57.4 
49.3 
53.1 
49.9 

136.0 
29.7 
18.4 
15.5 
15.3 
12.4 
12.2 
10.8 
10.3 
10.3 
10.0 
9.9 
9.9 
9.4 
9.3 
9.2 
9.2 
9.15 
87 
8.2 
8.8 
8/5 
11.1 
10.8 
8.9 
8.9 
8.7 
7.2 
9.2 
7.9 
8.5 
8.0 

13.596 
2.966 
1.84 
1.55 
.53 
.24 
.22 
.08 
.03 
.026 
.0 
0  994 
0.991 
0.94 
0.93 
0.92 
0.92 
0.159 
0.87 
0.82 
0.88 
0.85 
1.11 
1.08 
0.89 
0.89 
0.87 
0.72 
0.92 
0.79 
0.85 
0.80 

Bromine  

Sulphuric  acid  
Nitrous  acid  .  

Chloroform  

Water  of  the  Dead  vSea  
Nitric  acid  

Acetic  acid  

Milk 

Sea  water 

Pure  water  'distilled)  at  39°  F  .... 
Wine  of  Bordeaux    .  . 

Wine  of  Burgandy  .  .  .    . 

Oil,  linseed 

Oil.  popov 

Oil,  rape  seed 

Oil,  whale  

Oil,  olive  

Oil,  turpentine  . 

Oil,  potato    . 

Petroleum   . 

Naptha  

Ether,  nitric  

Ether,  sulphurous  

Ether,  nitrous 

Ether,  acetic  .... 

Ether,  hydrochloric  
Ether,  sulphuric  

Alcohol,  proof  spirit  

Alcohol,  pure 

Benzine  

Wood  Spirit  

440 


BATTLE      CREEK.     MICHIGAN.      U.  S.  A 


Circular  and  Angular  Measure 

60  seconds  (")  =  1  minute  (') 
60  minutes       =  1  degree  (°) 
360  degrees        =  1  circumference  (C) 

Cubic  Measure 

1728  cubic  inches  =  1  cubic,  or  solid  foot. 
27  cubic  feet      =  1  cubic,  or  solid  yard. 

A  pile  of  wood  cut  4  feet  long,  piled  4  feet  high,  8  feet  long  =  128  cubic 
feet  =  1  cord. 

A  porch  of  stone  =  16  ><  feet  long,  by  1  foot  high,  by  1^  feet  thick  =  24^ 
cubic  feet. 

A  perch  of  stone  =  22  cubic  feet  in  Philadelphia. 

A  perch  of  stone  =  16>£  cubic  feet  in  some  New  England  States. 

The  perch  is  so  variable  in  different  localities  that  it  should  never  be  used 
in  making  a  contract  unless  the  contents  in  cubic  feet  be  specified. 

A  ton  (2240  pounds)  of  Pennsylvania  anthracite,  when  broken  for  domestic 
use,  occupies  from  41  to  43  cubic  feet  of  space,  the  mean  of  which  is  equal  to 
1 . 556  cubic  yards,  or  a  cube  of  3.476  feet  on  each  edge. 

A  ton  (2240  pounds)  of  bituminous  coal  equals  44  to  48  cubic  feet,  mean 
equal  to  1.704  cubic  yards;  or  a  cube  of  3.583  feet  on  each  edge. 

A  ton  (2240  pounds)  of  coke  =  80  cubic  feet. 

A  cubic  foot  is  equal  to .1728  cubic  inches 

A  cubic  foot  is  equal  to 0.037037  cubic  yards 

A  cubic  foot  is  equal  to .  .  0.803564  U.  S.  struck  bushel  of  2150.42  cubic  inches 

A  cubic  foot  is  equal  to 32 1426  U  S  pecks 

A  cubic  foot  is  equal  to 7.48052  U.  S.  liquid  grilons  of  231  cubic  inches 

A  cubic  foot  is  equal  to  ...  6.42851  U.  S.  dry  gallons  of  268.8025  cubic  inches 

A  cubic  foot  is  equal  to 29.922C8  U.  S.  liquid  quarts 

A  cubic  foot  is  equal  to 25.71405  U.  S.  dry  quarts 

A  cubic  foot  is  equal  to 59.84416  U.  S.  liquid  pints 

A  cubic  foot  is  equal  to.  . .- 51 .42809  U.  S.  dry  pints 

A  cubic  foot  is  equal  to 239 . 37662  U.  S.  gills 

A  cubic  foot  is  equal  to 0.26667  flour  barrel  of  3  struck  bushels 

A  cubic  foot  is  equal  to. 0. 23748  U.  S.  liquid  barrel  of  31#  gallons 

A  cubic  yard  is  equal  to  7 . 2  flour  barrels  of  3  struck  bushels  each. 

A  ton  in  computing  the  tonnage  of  a  ship  or  other  vessel  is  100  cubic 
feet  of  their  internal  space. 

A  ton  in  computing  freight  on  ships  is  taken  at  40  cubic  feet  or  2240 
pounds,  at  the  ship's  option. 

Dry   Measure 

Edge  of  a  cube  of 
equal  capacity 

2  pints  =  1  quart 4.066  inches 

4  quarts  =  1  gallon  =  8  pints 6.454  inches 

2  gallons  =  1  peck  =  16  pints 8. 131  inches 

4  pecks  =  1  bushel  (struck)  =  64  pints  =32  quarts  =  8  gallons  ...  12 . 908  inches 

A  gallon  dry  measure  =  268 . 8  cubic  inches. 

A  bushel  dry  meaure  (same  as  British  Winchester  struck  bushel)  =2150.42 
cubic  inches,  or  77.63  pounds  avoirdupois  of  pure  water  at  its  maximum 
density. 

The  dimensions  of  a  bushel  by  law  are  18>^  inches  inner  diameter,  19K 
inches  outer  diameter,  and  8  inches  deep;  and  when  heaped,the  cone  is  not  to 
be  less  than  6  inches  high,  which  makes  a  heaped  bushel  equal  to  1M  struck 
bushels,  or  to  1 . 56  cubic  feet. 

A  struck  bushel  =  1.24  cubic  feet. 

The  dry  flour  barrel  =  3 . 75  cubic  feet  =  3  struck  bushels.  The  dry  barrel 
is  not  however,  a  legalized  measure. 

36  heaped  bushels  =  1  chaldron. 


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Measures    of    Length 

12  inches  =  1  foot. 
3  feet  =  1  yard  =  36  inches. 
5K"  yards  =  1  rod  =  198  inches  =  16K  feet. 
80  rods  =  1  furlong  =  7920  inches  =  660  feet  =  220  yards. 
4  furlongs  =  1  mile  =  63,360  inches  =  5280  feet  =  1760  yards  =320  rods. 

Gunter's   Chain 

(SOMETIMES  USED  IN  LAND  SURVEYING) 
7.92  inches  =  1  link. 
100  links  =  1  chain  =  4  rods  =  66  feet. 
80  chains  =  1  mile. 

Ropes  and  Cables 

6  feet  =  1  fathom;  120  fathoms  =  1  cable's  length. 

The  United  States  standard  yard  is  the  same  as  the  imperial  yard  of 
.jreat  Britain.  It  is  determined  as  follows;  The  rod  of  a  pendulum  vibrating 
econds  of  mean  time  in  the  latitude  of  London  in  a  vacuum  at  the  level  of 
he  sea  is  divided  into  391,393  equal  parts,  and  360,000  of  these  parts  are  36 
nches,  or  1  standard  yard. 

An  inch  is  one  500,500,000th  part  of  the  earth's  polar  axis. 

Artificers  sometimes  divide  the  inch  into  lines  or  twelfths,  but  more 
lommonly  into  binary  divisions — half,  quarter,  eighth,  sixteenth  and  thirty- 
econd. 

Mechanical  engineers  divide  the  inch  decimally — lOths,  lOOths,  lOOOths, 

:tC. 

Civil  engineers  divide  the  foot  decimally. 

A  nautical  mile,  geographical  mile,  sea  mile,  or  knot,  as  adopted  by 
Jnited  States  Coast  and  Geodetic  Survey,  is  equal  to  6080.27  feet. 

British  Admiralty  knot  =  6080  feet. 

A  geographical  or  nautical  mile  may  be  taken  =  1 . 15  statute  miles. 

The  league  =3  nautical  miles. 

The  geographical  degree  =  60  geographical  or  nautical  miles. 

Ths  length  of  a  degree  of  latitude  varies,  being  68 . 72  miles  at  the  equator, 
)9.C5  miles  in  middle  latitudes,  and  69.34  miles  in  the  polar  regions.  A  degree 
>f  longitude  is  greatest  at  the  equator,  where  it  is  69 . 16  miles,  and  it  gradually 
lecreases  toward  ths  poles,  where  it  is  0. 

1  hand  =4  inches. 

1  pace  =3  feet. 

The  hand  is  used  for  heights  of  horses  and  girths  of  spars. 

Square   or  Land   Measure 

144  square  inches  =  1  square  foot. 

9  square  feet  =  l  square  yard  =  1296  square  inches. 

3014  square  yards  =  I  square  rod  =2 72 ^square  feet. 

40  square  rods  =  1  rood  =  1210  square  yards  =  10,890  square  feet. 

4  roods  =  I  acre  =  160 square  rods  =  1840  square  yards  =  43,560  square  feet. 

A  section  of  land  =640  acres  =  1  square  mile. 

208.71  feet  square  =43. 560  square  feet  =  10  square  Gunter's  chains  =  1 
acre,  or  220  x  198  feet  =  1  acre. 

A  square  K-acre  is  147.58  feet  at  each  side;  or  110x198  feet. 

A  square  >£-  acre  is  104.355  feet  at  each  side;  or  55  x  198  feet. 

A  circular  acre  is  235.504  feet  in  diameter. 

A  circular  ^-acre  is  166.527  feet  in  diameter. 

A  circular  ><-acre  is  117.752  feet  in  diameter. 

A  circular  inch  is  a  circle  of  1-inch  diameter;  a  square  foot  =  183. 346 
:ircular  inches. 

1  square  inch  =  1.27324  circular  inches;  and  1  circular  inch  =0.7854  of 
i  square  inch. 


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United  States  Standard  Baume  Scale 

Relation  Between  Baume  Degrees  and  Specific  Gravity 
LIQUIDS  HEAVIER  THAN  WATER 


Baume 
Degrees 

Sp.  Gr. 
60°/60°F 

Baume 
Degrees 

Sp.  Gr. 
60°/GO°F 

Baume 
Degrees 

Sp.  Gr. 
60°/60°F 

Baume 
Degrees 

Sp.  G-. 
60J/60JF 

0.. 

1  

2  

1.00000 
1.00694 
1.01399 

20.. 
21  
22  

1.16000 
1.16935 

1.17886 

40  
41  
42  

1.38095 
1.39423 
1.40777 

60  
61  
62 

1.70588 
1.72619 
1.74699 

3  
4 

1.02113 
1.02837 

23  
24 

1.18852 
1.19835 

43  

44 

1.42157 
1  43564 

63..... 
64 

1.76829 
1  79012 

5.. 
6  

7  
8  

1.03571 
1.04317 
1.05072 
1.05839 

25.. 
26  

27  
28  

1.20833 
1.21849 

1.22881 
1.23932 

45  
46  
47  

48  

1.45000 
1.46465 
1.47959 
1.49485 

65  
66  
67  
68 

1.81250 
1.83544 
1.85897 
1.88312 

9  
10.  . 

1.06618 
1.07407 

29  
30 

1.25000 
1.26087 

49  

50 

1.51042 
1.52632 

69  
70 

1.90789 
1  93333 

11.  . 

1.08209 

31 

1.27193 

51 

1  54255 

71 

1  95946 

12  

1.09023 

32  

1.28319 

52  

1.55914 

72 

1.98630 

13.... 

1.09848 

33  

1.29464 

53  

1.57609 

73 

2.01389 

14.  . 

1.10687 

34 

1.30631 

51 

1  59341 

74 

2  04225 

15.. 

1.11538 

35.  . 

1.31818 

55.  . 

1.61111 

75 

2.07143 

16  

1.12403 

36  

1.33028 

56  

1.62921 

76 

2  10145 

17  

18  
19  

1.13281 
1.14173  ! 
1.15079 

37  ' 
1  38  
39  

1.34259 
1.35514 
1.36792 

57  

i  58  
59  

1.64773 
1.66667 
1.68605 

77  
78  
79  

2.13235 
2.16418 
2.19697 

LIQUIDS  LIGHTER  THAN  WATER 


10.. 

1.00000 

30.. 

0.87500 

50.. 

0.77778 

70.. 

0.70000 

11  

.99291 

31  

.86957 

51  

.77348 

71  

.69652 

12  

.98592 

32  

.86420 

52  

.76923 

72  

.69307 

13  

.97902 

33  

.85890 

53..... 

.76503 

73..... 

.68966 

14  

.97222 

34  

.85366 

54 

.76087 

74  

.68627 

15  

.96552 

35.. 

.84848 

55.  . 

.75676 

75 

.68293 

16  

.95890 

36  

.84337 

56 

.75269 

76  

.67961 

17  

.95238 

37  

.83832 

57 

.74866 

77 

.67633 

18  

.94595 

38  

.83333 

58  

.74468 

78  

.67308 

19  

.93960 

39  

.82840 

59 

.74074 

79 

.66986 

20.. 

.93333 

40.. 

.82353 

60  

.73684 

80.. 

.66667 

21  

.92715 

41  

.81871 

61  

.73298 

81 

.66351 

22  

.92105 

42  

.81395 

62  

.72917 

82 

.66038 

23  

.91503 

43  

.80925 

63 

.72539 

83 

.65728 

24  

.90909 

44  

.80460 

64 

.72165 

84 

.65421 

25.. 

.90323 

45  .... 

.80000 

65.  . 

.71795 

85.. 

.65117 

26  

.89744 

46  

.79545 

66  

.71428 

86  

.64815 

27  

.89172 

47  

.79096 

67  

.71066 

87  

.64516 

28  

.88608 

48  

.78652 

68  

.70707 

88  

.64220 

29  

.88050 

49  

.78212 

69  

.70352 

89  

.63927 

From  Circular  No.  59  Bureau  of  Standards. 


Table  of  Degrees  Brix 

Per  Cent.  Sugar  (Degrees  Balling.'s  or  Brix)  with  Corresponding 
Specific  Gravity  and  Degrees  Baume.     Temperature  60°  F. 


Per  Cent 

Per  Cent 

Per  Cent 

Sugar 
Balling's 
or  Brix 
60°  F— 

Specific 
Gravity 
60°/60°F 

Degrees 
Baume 
60°  F 

Sugar 
Balling's 
or  Brix 
60°  F— 

Specific 
Gravity 
60°/60°F 

Degrees 
Baume 
60°  F 

Sugar 
Balling's 
or  Brix 
60°  F— 

Specific 
Gravity 
60°/60°  F 

Degrees 
Baume 
60°  F 

15.56°  C. 

15.56°  C 

15.56°  C 

0 

1.0000 

0.00 

34 

1.1491 

18.81 

68 

1.3384 

36.67 

1 

1.0039 

0.56 

35 

1  .  1541 

19.36 

69 

1.3447 

37.17 

2 

1.0078 

1.13 

36 

1.1591 

19.90 

70 

1.3509 

37.66 

3 

.0118 

1.68 

37 

1  .  1641 

20.44 

71 

1.3573 

38.17 

4 

.0157 

2.24 

38 

1  .  1692 

20.98 

.72 

1.3636 

38.66 

5 

.0197 

2.80 

39 

1  .  1743 

21.52 

73 

1  .  3700 

39.16 

6 

.0238 

3.37 

40 

1  .  1794 

22.06 

74 

1  .  3764 

39.65 

7 

.0278 

3.93 

41 

1  .  1846 

22.60 

75 

1  .  3829 

40.15 

8 

.0319 

4.49 

42 

1  .  1898 

23.13 

76 

1.3894 

40.64 

9 

.0360 

5.04 

43 

1  .  1950 

23.66 

77 

1.3959 

41.12 

10 

.0402 

5.60 

44 

1.2003 

24.20 

78 

1.4025 

41.61 

11 

.0443 

6.15 

45 

.2057 

24.74 

79 

1.4091 

42.10 

12 

1.0485 

6.71 

43 

.2110 

25.26 

80 

1.4157 

42.58 

13 

1.0528 

7.28  ! 

47 

.2164 

25.80 

81 

1  .  4224 

43.06 

14 

1.0570 

7.81 

48 

.2218 

26.32 

82 

1.4291 

43.54 

15 

1.0613 

8.38 

49 

.2273 

26.86 

83 

1.4359 

44.02 

16 

1.0657 

8.94 

50 

.2328 

27.38 

84 

.4427 

44.49 

17 

1.0700 

9.49 

51 

1.2384 

27.91 

85 

1.4495 

44.96 

18 

1.0744 

10.04 

52 

1.2439 

28.43 

86 

.4564 

45.44 

19 

1.0788 

10.59 

53 

1.2496 

28.96 

87 

1.4633 

45.91 

20 

1.0833 

11.15 

54 

1  .  2552 

29.48 

88 

1  .  4702 

46.37 

21 

1  .  0878 

11.70 

55 

1  .  2309 

30.00 

.89 

1  .  4772 

46.84 

22 

.  0923 

12.25 

53 

1  .  2667 

30.53 

90 

.4842 

47.31 

23 

.0968 

12.80 

57 

1.2724 

31.05 

91 

.4913 

47.77 

24 

.1014 

13.35 

58 

1.2782 

31.56 

92 

.4984 

48.23 

25 

.1060 

13.90 

59 

1.2841 

32.08 

93 

.5055 

48.69 

26 

.1107 

14.45 

60 

1.2900 

32.60 

94 

.5126 

49.14 

27 

.1154 

15.00 

61 

1.2959 

33.11 

95 

.5198 

49.59 

28 

.1201 

15.54 

62 

1.3019 

33.63 

96 

.5270 

50.04 

29 

.1248 

16.19 

63 

1  .  3079 

34.13 

97 

.  5343 

50.49 

30 

1.1296 

16.63 

61 

1.3139 

34.64 

98 

1.5416 

50.94 

31 

1.1345 

17.19 

65 

1  .  3200 

35.15 

99 

1.5489 

51.39 

32 

1  .  1393 

17.73 

66 

1.3261 

35.66 

100 

1.5563 

51.93 

33 

1.1442 

18.28 

67 

1.3323 

36.16 

The  above  table  is  from  the  determinations  of  Dr.  F.  Plato,  and  has  been  adopted  as 
standard  by  the  United  States  Bureau  of  Standards. 


Pumps  for  the 
Oil  Industry 


/IL 


B  A T  T L  E      CREEK.     MI CSJLGAN ,     U.  S.  A. 


Petroleum  Fields 

The  American  Petroleum  industry  may  be  said  to  have 
had  its  inception  from  the  date  of  the  drilling  of  the  first  well 
in  1859.  Prior  to  this  date,  petroleum  had  been  obtained  in 
small  quantities  from  brine  wells  in  Pennsylvania,  and  from 
the  distillation  of  coal. 

The  Petroleum  fields  of  importance  in  the  United  States 
may  be  listed  as  follows: 

Appalachian 

Lima — Indiana 

Illinois 

Mid-Continent 

Central  and  Northern  Texas 

West  Texas 

Louisiana 

Gulf  Coast 

Wyoming 

California. 


Chemical  Properties  of  Petroleum 

Petroleum  is  a  mixture  of  chemical  compounds  of  carbon 
and  hydrogen  called  hydrocarbons  with  small  amounts  of 
sulphur,  nitrogen  and  oxygen.  These  last  three  usually  exist 
as  derivatives  of  the  hydrocarbons,  and  are  regarded  as  im- 
purities. Hydrogen  sulphide,  water  and  earthy  matter  are 
often  present  in  addition. 

The  elements  carbon  and  hydrogen  of  which  all  hydro- 
carbons are  composed,  possess  widely  different  properties. 
Carbon  which  is  one  of  the  most  widely  distributed  elements 
is  the  principal  component  of  all  organic  compounds.  Hydro- 
gen is  a  colorless,  odorless,  inflamable  gas  and  is  the  lightest 
substance  known. 


451 


1        UNION 

STEAM 

_P  U.M  P 

COM  P  ANY 

J 

Physical  Properties  of  Petroleum 

Specific  Gravity 

Petroleum  is  lighter  than  water.  The  specific  gravity  is 
influenced  by  physical  factors  and  by  the  chemical  composition 
of  the  crude  oil.  American  crude  petroleum  varies  in  specific 
gravity  from  .7684  to  .9960.  Russian  petroleum  from  .854  to 
.889  and  Mexican  oil  from  .975  to  .992.  In  practical  operation 
in  the  Petroleum  Industry,  the  specific  gravity  is  generally  ex- 
pressed in  terms  of  the  Baume  scale  which  bears  no  direct  rela- 
tion to  the  specific  gravity.  The  conversion  of  the  Baume 
scale  into  specific  gravity  is  as  follows: 

140 

Degrees  Baume  = — 130 

Sp.  Gr.  60°/60°  Fah. 

140 
Sp.  Gr.  60°/60°  Fah.  =  - 

130  +  deg.  Be 

Viscosity 

The  viscosity  or  measure  of  the  tendency  to  flow  is  an 
important  factor  with  lubricating  oils,  especially  when  it  comes 
to  handling  them  with  pumps.  It  is  usually  determined  as  the 
time  necessary  for  a  definite  volume  of  oil  at  a  definite  tempera- 
ture to  flow  through  a  small  opening  or  orifice.  This  work  is 
carried  out  in  an  instrument  known  as  a  viscosimeter  of  which 
there  are  several  standard  makes  in  use  at  the  present  time. 
All  of  them  utilize  the  same  general  principle.  Oil  is  heated 
in  a  metallic  cup,  surrounded  by  an  oil  bath.  The  temperature 
of  the  oil  in  the  cup  and  that  of  the  oil  bath  are  carefully  con- 
trolled; and  when  the  desired  temperature  has  been  reached,  a 
small  orifice  in  the  bottom  of  the  cup  is  opened,  and  the  oil  is 
allowed  to  flow  into  a  flask  of  known  capacity.  The  time 
necessary  for  the  flask  to  fill  is  taken  as  the  measure  of  the 
viscosity  of  the  oil. 

In  the  United  States,  the  Saybolt  standard  uniform  viscosi- 
meter is  generally  used.  The  Redwood  viscosimeter  is  used  in 
Great  Britain  and  in  Germany,  and  other  countries  the  Engler 
viscosimeter  is  used. 

The  time  in  seconds  for  the  delivery  of  60  cu.  in.  of  oil  is 
the  Saybolt  viscosity  of  the  oil  at  the  temperature  of  the  test 
which  generally  is  100°  Fah.,  150°  Fah.  or  210°  Fah. 

The  viscosity  of  fuel  oils  is  determined  by  the  Saybolt- 
Furol  Viscosimeter  at  temperatures  of  70°  Fah.  104°  Fah.  and 
122°  Fah. 


452 


It 

B 

ATT 

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C  RE 

EK. 

MIC 

HIG 

ATsT, 

U. 

s. 

^^ 

The  viscosity  of  oil  decreases  and  its  fluidity  increases  when 
the  temperature  is  raised.  This  is  important  as  it  has  every- 
thing to  do  with  the  successful  handling  of  it  with  pumps. 

Refining 

There  are  so  many  grades  of  crude  and  the  method  of  re- 
fining them  so  varied  that  only  an  outline  of  the  usual  practice 
will  be  given  .here. 

The  process  of  treating  crude  petroleum  is  always  one  of 
fractional  distillation  with  subsequent  chemical  treatment, 
filtering,  re-distillation  and  compounding  of  each  of  the  frac- 
tions. Often  only  one  treatment  is  necessary  to  produce  the 
desired  result;  often  two  or  more  steps  are  taken. 

There  are  three  major  classifications  of  petroleum, 

Paraffin  Base. 
Asphalt  Base. 
Mixed  Base. 

The  paraffin  base  crude  contains  very  little  asphalt.  Some 
of  the  well  known  paraffin  base  crudes  are  those  from  Pennsyl- 
vania, West  Virginia,  North  Louisiana,  Ranger,  Oklahoma  and 
Kansas. 

The  paraffin  base  crudes  are  most  valuable.  This  is  due 
not  alone  to  the  valuable  lubricating  oils  and  cylinder  stocks 
contained  therein,  but  also  to  the  fact  that  such  oils  show  a 
high  yield  of  gasoline. 

The  asphalt  base  crudes  leave  as  a  residue  a  heavy  pitch 
or  asphalt.  California,  certain  Texas  and  the  heavy  Mexican 
oils  are  of  this  class. 

A  mixed  base  petroleum  is  one  in  which  both  paraffin  and 
asphalt  are  found.  Illinois  and  some  of  the  light  Mexican  oils 
are  of  this  class. 

The  three  classes  of  crudes  are  handled  somewhat  similarly, 
but  the  yields  of  the  products  are  quite  different.  Paraffin  base 
oils  are  usually  run  with  every  effort  to  avoid  cracking  or  de- 
composition by  heat.  They  yield  the  bulk  of  our  high  grade 
lubricants.  Asphalt  base  crudes  on  the  other  hand,  will  yield 
greater  amounts  of  like  products  when  cracked.  These  oils  are 
generally  "topped"  for  the  lighter  fractions.  Mixed  base  oils 
are  usually  refined  by  combination  of  the  two  processes,  crack- 
ing and  non-cracking. 


453 


The  two  methods  employed  in  refining  petroleum  are 
straight  distillation  which  separates  the  compounds  of  different 
boiling  points  from  each  other  but  does  not  break  them  up,  and 
cracking  which  decomposes  or  breaks  up  the  oil  by  heating  it 
to  a  high  temperature. 

The  demand  for  gasoline  has  long  since  exceeded  the  avail- 
able supply  contained  in  the  crude  oil,  and  a  very  important  part 
of  the  refining  practice  today  consists  in  augmenting  the  natural 
supply  of  light  hydrocarbons  by -processes  of  decomposing  the 
heavier  oils  by  heat  treatment  and  thereby  obtaining  increased 
quantities  of  motor  fuel. 

Straight  Distillation 

The  crude  is  first  distilled  by  direct  firing  with  the  aid  of 
open  steam  sprays  in  the  still.  As  the  oil  is  heated  in  the  still, 
those  portions  of  low  boiling  points  vaporize  and  are  led  through 
condensing  coils  to  a  so-called  "look  box."  Here  the  stream  is 
under  observation  of  the  still  man  who,  by  means  of  samples, 
keeps  in  touch  with  the  operation.  As  the  temperature  of  the 
oil  in  the  still  rises,  fractions  of  high  boiling  points  and  higher 
gravity  are  vaporized  and  condensed,  and  flow  through  the  look 
box.  The  look  box.  is  connected  to  a  manifold  leading  to  the 
receiving  tanks,  one  or  more  tanks  being  provided  for  each  "cut" 
or  product  desired  from  the  distillation. 

The  cuts  or  separations  resulting  from  the  first  distillation 
of  a  paraffin  base  crude  will  run  about  as  follows: 

Crude  Naphtha  start .54°  Baume 

Kerosene  Distillate 54°-50°  Baume 

Crude  Kerosene 50°-38°  Baume 

Gas  Oil 38°-35°  Baume 

Wax  Distillate 35°  Baume 

The  crude  naphtha  or  first  cut  is  the  base  of  commercial 
naphthas  and  gasoline.  The  distillate  will  cont'ain  hydrocar- 
bons of  higher  boiling  points  than  are  allowable  in  gasoline. 
Further  distillation  is  therefore  required,  and  this  is  carried  out 
in  steam  stills  with  dephlegmating  towers  so  the  lighter  consti- 
tuents of  the  crude  naphtha  can  escape.  In  this  distillate  75 
to  80%  of  the  charge  will  pass  over  as  commercial  grades  of 
gasoline.  The  residual  which  is  naphtha  bottoms  is  further 
distilled  with  kerosene  stocks. 


454 


r&^^^Jr^^&^^&^J^&S^^^Si^^S^' 


The  kerosene  distillate,  like  the,  naphtha  cut,  contains  pro- 
ducts which  are  more  homogeneous.  The  distillate  is  treated 
in  steam  stills  as  before  and  run  down  to  the  desired  flash  point. 
The  distillate  which  is  carried  over  is  put  into  the  crude  naphtha 
cut  from  the  crude  oil  distillation  for  further  handling. 

The  crude  kerosene  from  the  still  and  naphtha  bottoms  are 
then  treated  and  represent  various  grades  of  kerosene  oils. 

Gas  oil  is  usually  marketed  as  obtained  from  the  crude  fire 
still.  It  is  sometimes  blended  with  heavier  oils  for  producing 
certain  grades  of  fuel  oil.  It  is  also  used  in  the  cracking  pro- 
cesses. The  wax  distillate  which  is  taken  from  the  crude  still 
contains  many  compounds  of  the  solid  paraffin  series  and  aho 
valuable  oils  from  which  high-grade  lubricants  are  made.  It 
is  again  subjected  to  distillation  which  changes  the  character  of 
the  wax  to  a  crystalline  form  which  enables  it  to  be  extracted. 
The  resulting  cracked  distillate  is  chilled  by  refrigerating  ma- 
chines and  then  pumped  through  a  filter  press  to  remove  the 
wax.  The  pressed  oil  is  fire-stilled  with  bottom  steam,  the 
residual  in  the  still  resulting  in  a  lubricating  oil  stock.  The 
overhead  distillates  can  then  be  fractionated,  and  when  treated 
become  the  various  grades  of  automobile,  air  compressor  and 
engine  oils.  The  wa'x  taken  from  the  distillate  is  sweated  and 
purified,  and  becomes  the  commercial  paraffin  wax. 

Cracking 

The  decomposition  of  petroleum  with  the  consequent 
breaking  up  of  the  molecules,  and  the  production  of  both  lighter 
and  heavier  hydrocarbons  .is  called  "cracking."  In  the  oil 
industry,  cracking  processes  are  those  designed  to  utilize  the 
above  decomposition  for  the  conversion  of  heavier  oils  into  the 
more  valuable  gasolines  and  naphthas.  All  petroleum  hydro- 
carbons have  a  characteristic  temperature  above  which  the 
cracking  reaction  takes  place.  This  temperature  varies  for 
the  different  cuts  from  the  given  crude  and  for  similar  cuts 
from  different  crude  oils.  For  the  gas  oil  and  fuel  oil  distillates 
now  in  use  as  stock  for  cracking  operation,  the  temperature 
necessary  to  cause  the  re-action  is  usually  between  550°  Fah. 
and  600°  Fah. 

The  great  bulk  of  the  stocks  which  are  cracked  for  yields 
of  gasoline  is  composed  of  gas  oils,  and  the  stocks  distilled  from 
crude  oil  between  that  cut  and  coke.  There  are  two  essential 
factors  in  the  cracking  operation:  temperature  and  the  .time 


AN  D    C  ON  D  E  N  S  E  R  S    P     R   E  VE  RV_ 5  E RVTCE 


455 


through  which  the  molecule  is  subjected  to  that  temperature. 
Pressure  is  corollary  to  the  temperature.  The  simpler  hydro- 
carbons require  higher  temperatures  and  longer  time  than  the 
more  complex  ones  of  greater  specific  gravity.  Such  stocks  as 
kerosene  distillate  are  therefore  seldom  cracked  on  a  commercial 
scale. 

The  systems  in  commercial  use  may  be  broadly  classified 
as  cracking  in  the  vapor  phase  and  cracking  in  the  liquid  phase. 

Cracking  in  the  vapor  phase  consists  in  vaporizing  the  oil 
and  then  producing  the  re-action  by  the  addition  of  heat,  or  of 
heat  and  pressure  together.  Temperatures  ordinarily  used  are 
from  1000°  Fah.  up,  although  it  is  possible  to  operate  vapor 
phase  cracking  at  as  low  a  temperature  as  750°  Fah.  Among 
the  various  processes  which  have  been  experimented  upon  in 
vapor  phase  are  the  Rittman,  Gyro,  Greenstreet  and  Ellis. 

The  majority  of  commercial  processes  in  general  use  are 
on  the  liquid  phase  principle  where  the  heat  is  applied  to  the 
liquid  under  very  high  pressure  sufficient  to  keep  it  liquid.  The 
processes  in  use  are  the  Tube  and  Tank,  Cross,  Holmes-Manley, 
Dubbs,  Fleming,  Isom,  Coast  and  Emerson.  There  are  also 
many  other  processes  but  no  attempt  will  be  made  here  to  de- 
scribe them. 

Casing  Head  Gasoline 

Gasoline  is  also  obtained  from  casing  head  gas  which  flows 
from  oil  wells  between  the  tubing  and  the  casing.  There  are 
two  methods  of  handling  this  gas  in  the  production  of  gasoline : 
by  the  compression  method  and  by  the  absorption  method. 

When  the  gas  is  rich,  it  is  compressed  by  a  two-stage  com- 
pressor at  a  pressure  from  50  to  300  Ibs.  and  flows  through  a 
series  of  water-cooled  condenser  coils  in  which  the  casing  head 
gasoline  separates  and  is  collected  in  tanks,  while  the  non-con- 
densable vapors  are  piped  away. 

The  absorption  process  is  used  where  the  gas  yields  less 
than  l]/2  gallons  of  gasoline  per  1000  cubic  feet.  This  process 
involves  passing  casing  head  gas  under  pressure  through  a  heavy 
oil  in  which  the  heavier  constituents  of  the  gas  are  dissolved  and 
retained  by  the  heavy  oil.  By  steam  distillation  of  the  heavy 
oil,  the  casing  head  gasoline  is  recovered. 


____AJMR._ 
456 


AND    CONDENSERS    FOR   EVERV  SERVICE 


457 


Pumps  for  the  Oil  Industry 

In  probably  no  other  enterprise  in  the  universe  do  pumps 
play  such  an  important  role  as  in  the  oil  industry.  Pumps 
contribute  to  the  success  of  every  phase  of  this  great  industry: 
production,  transportation  of  the  crude,  refining,  transportation 
of  the  finished  products  and  marketing. 

When  the  oil  industry  was  in. its  infancy,  little  attention 
was  paid  to  the  economy  and  dependability  of  the  pumping 
equipment,  but  with  the  gradual  development  of  the  industry, 
the  resulting  competition,  and  the  narrowing  margins  of  profit, 
it  has  been  found  that  economical  and  dependable  pumping 
equipment  are  absolutely  essential.  Realizing  the  exacting 
service  required  of  pumping  equipment  for  the  oil  industry,  and 
the  necessity  of  having  pumps  built  for  each  particular  service, 
the  Union  Steam  Pump  Company  has,  over  a  long  period  of 
years,  developed  a  complete  line  of  pumps  for  this  particular 
field. 

A  few  of  the  many  different  types  of  pumps  for  the  oil  in- 
dustry are  shown  on  the  following  pages. 

For  general  water  supply,  cooling  towers,  boiler  feed,  etc., 
Simplex,  Duplex,  also  Centrifugal  pumps  are  used.  See  page  461. 

Light  oils  such  as  gas  oil,  gasoline,  naphtha  kerosene,  etc., 
are  generally  handled  "by  specially  fitted  pumps  of  the  Simplex, 
Duplex  or  Centrifugal  types  as  shown  on  oages  461  and  464. 

For  oil  such  as  heavy  crude  residiums,  specially  designed 
pumps  are  necessary  with  liberal  valve  and  port  openings.  The 
separate-chest  pattern  pump  shown  on  page  461  is  a  special 
type  pump  for  this  service. 

For  oil-line  pumping,  where  the  pressures  to  be  met  are 
around  750  to  1000  Ibs.,  a  specially  designed  pump  is  used  of 
the  duplex  type,  as  shown  on  page  462.  The  Duplex  plunger 
type  of  pump  shown  on  page  463  is  also  used  for  this  service. 

For  pumping  oils  against  high  pressures,  also  for  charging 
stills  where  the  temperatures  are  not  excessive,  the  plunger 
pumps  shown  on  pages  462  and  463  are  used. 

When  it  comes  to  the  question  of  handling  hot  oils,  the  type 
of  pump  to  use  depends  not  only  on  the  temperature  but  the 
pressure,  the  gravity  of  the  oil,  and  the  suction  conditions. 
Every  condition  is  different,  so  no  definite  statement  can  ba 


made  as  to  the  exact  type  to  use  until  a  careful  study  is  made 
of  the  conditions. 

In  general,  pumps  for  hot-oil  service  may  be  classed  as 
piston  and  plunger  types. 

The  piston  type  is  designed  and  built  in  the  valve  pot 
pattern,  Simplex,  Duplex  and  Twin,  with  semi-steel  and  cast 
steel  fluid  ends.  See  pages  465  to  467.  And  for  extreme  con- 
ditions for  temperatures  up  to  1000°,  the  piston  pattern  is  fur- 
nished in  the  Simplex,  Duplex  and  Twin  types  with  forged  steel 
fluid  ends  and  cooled  stuffing-boxes.  See  pages  468  to  470. 

For  pressures  up  to  3500  Ibs.,  and  for  temperatures  up  to 
1000°,  the  specially  designed  forged-steel  plunger  pump  in  the 
Simplex  or  Twin  with  cooled  plungers  and  stuffing-boxes  shown 
on  pages  471  and  472  is  furnished. 

For  handling  heavy  viscous  oils  like  acid  sludge,  we  furnish 
a  specially  designed  type  of  pump  shown  on  page  474  with  fluid 
ends  made  of  iron  or  acid-resisting  bronze. 

For  fire  protection,  the  *Foamite  type  of  pump  is  used  as 
shown  on  page  473.  This  pump  is  a  special  type  arranged  for 
handling  two  different  solutions;  one  solution  consisting  of  a 
viscous  material  and  bicarbonate  of  soda  and  the  other  con- 
taining aluminum  sulphate.  When  these  two  solutions  are 
brought  together  in  equal  parts,  they  will  form  a  foam,  whose 
volume  is  seven  to  eight  times  the  combined  original  volumes  of 
the  two  liquids,  which  is  utilized  in  extinguishing  fires. 

For  cargo  loading,  we  build  a  special  pump  of  the  valve 
pot  type  as  shown  on  page  474. 

In  addition  to  the  types  of  pumps  shown,  we  make  a  com- 
plete line  of  power  pumps  which  are  specially  designed  for 
practically  all  the  various  services  mentioned  above. 

Twin  Pumps 

The  Twin  pumps  referred  to  herein  and  shown  on, the  fol- 
lowing pages  are  a  special  type  which  we  originated.  The  Twin 
pump  consists  of  two  Burnham  single  pumps  taking  steam 
through  a  patented  synchronizing  valve,  which  device  keeps 
the  two  pumps  in  step,  one  pump  reversing  when  the  other  is 
at  about  mid-stroke.  The  synchronizing  valve  is  functioned  by 
the  auxiliary  pistons  carrying  the  main  steam  valve  of  the  two 


459 


U  N  I  O  N       STEAM       PUMP CO  MPANY 


companion  pumps,  and  this  mechanism  is  entirely  independent 
of  the  valve  gear  which  controls  the  stroke  of  the  two  pumps. 

The  Burnham  twin  mechanism  is  a  simple  device  by  means 
of  which  it  is  possible  for  us  to  furnish  a  pumping  unit  which  is 
particularly  adapted  to  handling  oils.  A  few  of  the  many 
advantages  of  this  pump  are : 

A  pump  with  a  very  uniform  discharge  which  is  essen- 
tial. 

Flexibility,  which  is  of  paramount  importance  for  a 
pump  for  this  service. 

The  pump  may  be  operated  as  a  twin  or  in  case  of  re- 
packing, repairs,  etc.,  either  side  of  the  unit  may  be  shut 
down,  the  other  continuing  to  run  at  practically  double 
the  speed. 

By  utilizing  the  Burnham  Simplex  steam  end,  it  is  pos- 
sible to  obtain  a  high  degree  of  economy  which  is  character- 
istic of  that  pump. 

Since  each  pump  is  operated  by  its  own  valve  gear, 
there  is  no  possibility  of  short-stroking  as  the  pump  must 
take  its  full  stroke  before  it  can  reverse.  This  feature  is 
particularly  desirable  for  handling  oils,  also  if  the  pump 
should  be  used  as  a  meter. 


1 


460 


~A  T  T  L  E ,      C :  R E  E  K .     Ml C 


Fig.  103a.     General  Service  Duplex  Pump  for  Light  Oils  and  Water. 


Fig.  95.     General  Service  Simplex  Pump  for  Light  Oils  and  Water. 


Fig.  205.     Separate-Chest  Pattern  Duplex  Pump  for  Handling  Heavy  Oil. 


o  N 


'  X  M     p  LTM  "p 


PA  .N  Y 


Fig.  210.     Duplex  Oil  Line  Pump,  6  and  8"  stroke. 


Fig.  181.     Duplex  Oil  Line  Pump,  10"  and  12"  stroke. 


Fig.  211.     Simplex  Plunger  Pump.     For  Handling  Oils  Against  High 
Pressures,  also  for  Charging  Stills  at  Moderate  Temperatures. 


PUMPING    MACHINERY,    AIR   COMPRE  S  S  OR  S 

W  Tonj"ETfTr\if  jj*  wy  vrvww  w  w  TJV  wryy_"wir  !BJIL!tf  y  T  g  P  g  nr  nf  g  mwtfyyTftTT'fl'Tg  vrw  w  a  *a  ^  w  w  ^  •ff~^'>"^~i:'  "gin  -*-$-ww  •* 


462 


463 


UNION       STEAM       PUMP       C  O  M  PANY 


as^^cp 

Y~ 


Fig.  86. 

Motor-Driven  Pump.     For  Circulating  Light  Oils,  Water,  etc. 


Fig.  213. 
Motor-Driven  Gasoline  Pump. 


Fig.  214. 

Multistage  Steam  TurDme-Driven  Centrifugal  Pump.    For  High  Pressure 
Oil  or  Water,  also  for  Boiler  Feeding. 


^R 

JMPING 

MAC 

HINERY, 

AIR 

COMPRESSORS 

aJl 

464 


Fig.  215. 
Burnham  Valve-Pot  Pattern  Simplex  Hot  Oil  Pump. 


Fig.  216. 
Duplex  Valve-Pot  Pattern  Hot  Oil  Pump. 


AND    CONDENSERS    FOR    EVERV   SERVICE 


465 


a 

I 
§ 

.+-> 


466 


467 


UNION       STEAM       PUMP 


C  O  M  PANV        ill 


Fig.  218. 
Simplex  Forged-Steel  Hot  Oil  Pump,  Piston  Pattern, 


Fig.  219. 

Simplex  Forged-Steel  Hot  Oil  Pump,  Piston-Pattern  with  Compound 
Steam  End. 


PUMPING    MACHINERY,    AIR   COMPRESSORS 


468 


LJLULK3C 

A.TTL 


MICHIGAN,      U.S.A. 


AND    CONDENSERS    FOR   EVERV  SERVICE 

"~  ''' '~ "''" 


469 


UNION       STEAM       PUMP       COMPANY 


470 


B  A  T  t  L  _E~ 


c 

g 

Q 

a 

c 
O 


o 


PUMPING    MACHINERY.    AIR   COMPRESSO 


472 


AND    CONDENSERS    FOR   EVERT  S 


473 


Fig.  225. 
Pump  for  Heavy  Oils,  Sludge,  etc. 


Fig.  182. 
Cargo  Loading  Pump. 


474 


Useful  Information — Oil 


1    Barrel  equals  42  U.  S.  gals. 

1  Barrel  per  hour  equals  .7  U.  S.  gals,  per 
minute. 

Barrels  per  hour  x  .7  equals  gals,  per  min- 
ute. 

Gals,  per  minute  divided,  by  .7  equals  bar- 
rels per  hour. 

Barrels  per  hour  x  24  equals  barrels  per  day. 

1  Barrel  per  day  equals  .0292  gals,  per 
minute. 

Barrels  per  day  x  .0292  equal  gals,  per  min- 
ute. 

Gals,  per  minute  divided  by  .0292  equals 
barrels  per  day. 

Number  of  barrels  in  pipe  one  mile  long 
equals  diameter  of  pipe  in  inches  squared 


Velocity  in  feet  per  second  equals  .0119  x 
barrels  per  day  divided  by  diameter  of 
pipe  in  inches  squared,  or  Velocity  equals 
.2856  x  barrels  per  hour  divided  by  the 
diameter  of  pipe  in  inches  squared,  or 
Velocity  equals  .408  x  gals,  per  minute 
divided  by  the  diameter  of  pipe  in  inches 
squared. 

Net  Horse  Power  equals  the  theoretical  horse 
power  necessary  to  do  the  work. 

Net  Horse  Power  equals  barrels  per  day  ? 
Pressure  x  .000017. 

Net  Horse  Power  equals  barrels  per  hour 
x  Pressure  x  .000408. 

Net  Horse  Power  equals  gals,  per  minute 
x  Pressure  x  .000583. 


CHARACTERISTICS  OF  TESTED  OILS 

OILS    TESTE  D 

GRAVITY 

Pounds 
per 

Gallon 

Degrees 
Beaume 

Specific 
Gravity 

California,   Bakersfield  -  
Louisiana,  Jennings  

16.0 
24.0 
37.0 
28.0 
24.0 
32.2 
36.2 
35.4 
43.7 
38.2 
29.0 
22.0 
20  0 
18.0 
27.9 
40.0 

.9595 
.9105 
.8395 
.8870 
.9105 
.8631 
.8423 
.8464 
.8059 
.8323 
.8815 
.9220 
.9340 
.9465 
.8866 
.8250 

7.994 
7.585 
6.994 
7.390 
7.585 
7.198 
7.023 
7.055 
6.722 
6.944 
7.344 
7.681 
7.781 
7.885 
7.394 
6.873 

Oklahoma  Residuum                   -  

"          Crude   (G   P   ) 

Russian,  Baku                                       -  

'     ,  Residuum  :  ..  
Gas  Oil 

West  Virginia                                        -         

FRICTION  LOSS  IN  OIL  PIPE  LINES 

The  friction    loss    in  oil  pipe  lines  may  be  found  by  the  following  formula: 
CXB2 


F=- 


In   which 


10XD5 


F  =  Friction  in  pounds  per  square  inch  per  mile  (5280    feet.) 

C  =  A  Constant  from  the  table  below  which  depends  on  the  character  of  the  oil. 

B  =  Barrels  of  oil  per  hour. 

D  =  Diameter  of  pipe  in  inches. 

TABLES  COMPUTED  FOR  33°  BEAUME 

When  "F"  is  given  and  "B"  computed,  add  1%  to  "B"  for  every  3°  above  and  subtract 
1%  from  ''B''  for  every  3°  below:  When  ''B''  is  given  and  ''F''  computed,  subtract  2% 
from  "F"  for  every  3°  above  and  add  2%  for  every  3°  below — or  interpolate  for  9.00 


CONSTANTS  FOR  DIFFERENT  OILS 


1/3    D 

in   <u 

03    <L> 

tst  a 

£§ 

4J 

<L>    C 

gi 

"w 

to 

t/j 

Mrt 

C                  ! 

&0  rt 

60  cfl 

C 

&  i 

c 

.33 

U          1 

o£ 

O 

<U   a) 

QPQ 

-  0 

O 

<U   <y 

Qpq 

O 

O 

l 

1 

65 

7   38 

53 

8.10 

41 

8.82 

29 

9.54 

62 

7.55 

50 

8.28 

38 

9.00 

26 

9.72 

59 

7.74 

47 

8.46 

35 

9.18 

23 

9.90 

5(3 

7.92 

41 

8.64 

32 

9.36 

20 

10.08 

Using  9  .00  as  a  CONSTANT  for  38°  oil,  subtract  .06  for  each  degree  above  38°,  and  add 
.06    for    each   degree    below    38°. 

For  every  10  degrees  above  60  degrees  Fahrenheit,  subtract  1°  from  the  Beaume  reading, 
and  for  every  10  degrees  below  60  degrees  Fahrenheit  add  1°  to  the  Beaume  reading; 
For    Example: — 

Raise  38°  Bme  oil  from  60°  F  to  80°F;  then  80—60  =  20  and  20 -=-10  =  2:  and  38—2  =  36 
or  36°  Bme  the  new  Beaume  reading  for  36°  Bme  Oil  heated  from  60  °F  to  80°F. 


AND 

CONDEN 

SERS 

FOR 

EVERY 

SERVICE 

; 

475 


Characteristics  of  American  Petroleum  Oils 


U.  S.  Bureau 

U.  S.  Bureau 

of  Standards 

A.  P.  I. 

o 

of  Standards 

A.  P.  I. 

O 

d 

d 

i 

I 

I 

g* 

6 

1. 

a    .£*! 

rt 

n 

0  >* 

|| 

II 

tJ  C 

c  o 

§i 

03 

m 

0  -^ 

oj 

II 

-t  g 

n 

i 

O  M 

II 

§^ 

rt 

d£ 

S5 

Q 

wO 

fSo 

1,2 

£o 

«i 

10.0 

1.0000 

8.325 

1.0000 

8.331 

.00035 

30.0 

0.8750 

7.286 

0.8762 

7.300 

.00036 

10.5 

.9964 

8.299 

.9965 

8.302 

.00035 

30.5 

.8723 

7.264 

.8735 

7.277 

.00037 

11.0 

.9929 

8.269 

.9930 

8.273 

.00035 

31.0 

.8696 

7.241 

.8708 

7.255 

.00037 

11.5 

.9894 

8.240 

.9895 

8.244 

.  00035 

31.5 

.8669 

7.218 

.8681 

7.232 

.00037 

12.0 

.9859 

8.211 

.9861 

8.215 

.  00035 

32.0 

.8642 

7.196 

.8654 

7.210 

.  00037 

12.5 

.9825 

8.182 

.9826 

8.186 

.  00035 

32.5 

.8615 

7.173 

.8628 

7.188 

.00037 

13.0 

.9790 

8.153 

.9792 

8.158 

.  00035 

33.0 

.8589 

7.152 

.8602 

7.166 

.  00037 

13.5 

.9756 

8.125 

.9759 

8.130 

.  00035 

33.5 

.8563 

7.130 

.8576 

7.145 

.00037 

14.0 

.9722 

8.096 

.9725 

8.102 

.  00035 

34.0 

.8537 

7.108 

.8550 

7.123 

.  00037 

14.5 

.9688 

8.069 

.9692 

8.074 

.00035 

34.5 

.8511 

7.087 

.8524 

7.104 

.  00037 

15.0 

.9655 

8.041 

.9659 

8.047 

.  00035 

35.0 

.8485 

7.065 

.8498 

7.080 

.00037 

15.5 

.9822 

8.013 

.9626 

8.019 

.00035 

35.5 

.8459 

7.044 

.8473 

7.059 

.00037 

16.0 

.9589 

7.986 

.9593 

7.992 

.00035 

36.0 

.8434 

7.022 

.8448 

7.038 

.  00037 

16.5 

.9556 

7.959 

.9561 

7.965 

.  00035 

36.5 

.8408 

7.001 

.8423 

7.017 

.  00037 

17.0 

.9521 

7.931 

.9529 

7.939 

.00035 

37.0 

.8383 

6.980 

.8398 

6.996 

.  00037 

17.5 

.9492 

7.904 

.9497 

7.912 

.  00035 

37.5 

.8358 

6.960 

.8373 

6.976 

.00037 

18.0 

.9459 

7.877 

.9465 

7.885 

.  00035 

38.0 

.8333 

6.939 

.8348 

6.955 

.00038 

18.5 

.9428 

7.851 

.9433 

7.859 

.00035 

38.5 

.8309 

6.918 

.8324 

6.935 

.00038 

19.0 

.9396 

7.825 

.9402 

7.833 

.  00035 

39.0 

.8284 

6.898 

.8299 

6.914 

.00038 

19.5 

.9365 

7.799 

.9371 

7.807 

.  00035 

39.5 

.8260 

6.877 

.8275 

6.894 

.00038 

20.0 

.9333 

7.772 

.9340 

7.781 

.  00036 

40.0 

.8235 

6.857 

.8251 

6  .  S74 

.00038 

20.5 

.9302 

7.747 

.9309 

7.755 

.00036 

40.5 

.8211 

6.837 

.8227 

6.854 

.  00039 

21.0 

.9272 

7.721 

.9279 

7.730 

.  00036 

41.0 

.8187 

6.817 

.  8203 

6.834 

.  00039 

21.5 

.9241 

7.696 

.9248 

7.705 

.00036 

41.5 

.8163 

6.797 

.8179 

6.814 

.  00039 

22.0 

.9211 

7.670 

.9218 

7.680 

.  00036 

42.0 

.8140 

6.777 

.8156 

6.795 

.00039 

22.5 

.9180 

7.645 

.9188 

7.655 

.00036 

42.5 

.8116 

6.758 

.8132 

6.775 

.  00039 

23.0 

.9150 

7.620 

.9159 

7.630 

.00036 

43.0 

.8092 

6.738 

.8109 

6.756 

.00039 

23.5 

.9121 

7.595 

.9129 

7.605 

.00036 

43.5 

.8069 

6.718 

.8086 

6.736 

.00039 

24.0 

.9091 

7.570 

.9100 

7.581 

.00036 

44.0 

.8046 

6.699 

.8063 

6.717 

.00039 

24.5 

.9061 

7.546 

.9071 

7.557 

.  00036 

44.5 

.8023 

6.680 

.8040 

6.698 

.  00039 

25.0 

.9032 

7.522 

.9042 

7.533 

.  00036 

45.0 

.8000 

6.661 

.8017 

6.679 

.  00039 

25.5 

.9003 

7.497 

.9013 

7.509 

.  00036 

45.5 

.7977 

6.642 

.7994 

6.660 

.  00039 

.26.0 

.8974 

7.473 

.8984 

7.485 

.  00036 

46.0 

.7955 

6.623 

.7972 

6.641 

.  00039 

26.5 

.8946 

7.449 

.8956 

7.461 

.  00036 

46.5 

.7932 

6.604 

.7949 

6.623 

.  00040 

27.0 

.8917 

7.425 

.8927 

7.437 

.  00036 

47.0 

.7910 

6.586 

.7927 

6.604 

.  00040 

27.5 

.8889 

7.402 

.8899 

7.414 

.00036 

47.5 

.7887 

6.567 

.7905 

6.586 

.  00040 

28.0 

.8861 

7.378 

.8871 

7.390 

.00036 

48.0 

.7865 

6.548 

.7883 

6.567 

.00040 

28.5 

.8833 

7.355 

.8844 

7.378 

.00036 

48.5 

.7843 

6.530 

.7861 

6.549 

.  00040 

29.0 

.8805 

7.332 

.8816 

7.345 

00036 

49.0 

.7821 

6.511 

.7839 

6.531 

.  00041 

29.5 

.  8777 

7.309 

.8789 

7.322 

00036 

49.5 

.7799 

6.494 

.7818 

6.513 

.00041 

^ 


476 


BATTLE      CREEK.     MICHIGAN.      U.S.A. 


Friction  of  Oil  '  -       38°  Beaume 
Pounds  Per  Square  Inch  in  Pipes  1  Mile  Long 


Barrels 
per  Hour 

JJlAMJiiliK  Ur  .Firr/ 

2" 

3" 

4* 

5" 

6* 

8" 

10" 

10 

2.8 

.37 

.088 

.0288 

.0116 

.00274 

.  00091 

15 

6.2 

.83 

.198 

.063 

.026 

.0064 

.  00203 

20 

11.2 

1.48 

.352 

.115 

.0462 

.011 

.0036 

25 

17.6 

2.3 

.55 

.18 

.0725 

.0172 

.0056 

30 

25.3 

3.32 

.792 

.26 

.104 

.0247 

.0081 

35 

34.5 

4.52 

1.08 

.353 

.142 

.0337 

.0112 

40 

45.0 

5.9 

1.43 

.46 

.185 

.044 

.0144 

45 

57.0 

7.49 

1.78 

.58 

.235 

.0556 

.0181 

50 

70. 

9.24 

2.2 

.72 

.29 

.0686 

.0225 

55 

85. 

11.2 

2.26 

.87 

.35 

.084 

.0273 

60 

101. 

13.3 

3.16 

1.04 

.416 

.099 

.0325 

65 

118.4 

15.6 

3.72 

1.22 

.49 

.116 

.0381 

70 

138. 

18.1 

4.3 

1.41 

.568 

.136 

.0442 

75 

158. 

20.8 

4.95 

1.62 

.651 

.155 

.0508 

80 

180. 

23.6 

5.62 

1.84 

.74 

.176 

.0578 

85 

203. 

26.7 

6.35 

2.08 

.836 

.  .198 

.0652 

90 

227. 

30.0 

7.11 

2.33 

.939 

.224 

.073 

95 

253. 

33.4 

7.92 

2.6 

1.045 

.248 

.0814 

100 

280. 

37.0 

8.8 

2.88 

1.16 

.275 

.0902 

125 

440. 

57.8 

13.7 

4.5 

1.81 

.43 

.142 

150 

630. 

83.0 

19.8 

6.5 

2.6 

.618 

.203 

175 

113.0 

27.0 

8.8 

3.54 

.84 

.275 

•  200 

148.0 

35.2 

11.5 

4.63 

1.1 

.36 

225 

187. 

42.5 

14:6 

5.85 

1.39 

.455 

250 

230. 

55.0 

18.0 

7.22 

1.72 

.56 

275 

280. 

66.5 

21.7 

8.75 

2.08 

.68 

.300 

332. 

79.2 

26.0 

10.4 

2.47 

.81 

325 

390. 

93.0 

30.4 

12.2 

2.9 

.95 

350 

453. 

10.2 

35.3 

14.2 

3.37 

1.12 

375 

124. 

40.5 

16.3 

3.85 

1.26 

400 

141. 

46.0 

18.5 

4.4 

1.44 

425 

159. 

52.0 

20.9 

4.96 

1.63 

450 

178. 

58.2 

23.5 

5.56 

1.83 

475 

198. 

65.0 

26.1 

6.25 

2.04 

500 

220. 

72.0 

28.9 

6.88 

2.25 

525 

242. 

79.5 

31.9 

7.58 

2.48 

550 

266. 

37.0 

35.0 

8.3 

2.73 

ANDCONDENSERS    FOR   EVERY  SERVICE 


1 

U  N 

I  ON 

STE 

AM 

P 

U  M 

P 

CO 

M 

PANY 

1 

Friction  of  Oil 


38°  Beaume 


Pounds  Per  Square  Inch  in  Pipes  1  Mile  Long 

(Continued) 


Barrels 
per   Hour 

Diameter  of  Pipe 

|     Barrels 
per  Hour 

Diameter  of  Pipe 

5" 

6" 

8" 

10" 

8* 

10" 

550 

87.0 

35.0 

8.3 

2.72 

3600             356 

117 

575 

95.0 

38.4 

9.1 

2.98 

3800 

397 

130 

600 

104 

41.7 

9.9 

3.24 

4000 

440 

144 

625 

112 

45.4 

10.7 

3.5 

4200 

158 

650 

122 

49.0 

11.6 

3.8 

4400 

174 

675 

131 

53.0 

12.5 

4.1 

4600 

192 

700 

141 

56.9 

13.5 

4.42 

4800 

207 

725 

152 

61.0 

14.4 

4.73 

5000 

225 

750 

162 

65.3 

15.5 

5.06 

5200 

243 

775 

173 

69.8 

16.5 

5.41 

5400 

262 

600 

184 

74.3 

17.6 

5.76 

5600 

282 

825 

196 

79.0 

18.7 

6.12 

5800 

303 

850 

208 

83.9 

19.8 

6.5 

6000 

324 

875 

221 

88.8 

21.1 

6.89 

6200 

346 

900 

233 

94.0 

22.3 

7.3 

6400 

368 

925 

247 

99.2 

23.5 

7.7 

6600 

392 

950 

260 

104.5 

24.8 

8.12 

6800 

416 

975 

274 

111.0 

26.2 

8.55 

7000 

441 

1000 

288 

115.8 

27.5 

9.0 

1100 

348 

140.0 

33.2 

10.9 

1200 

415 

166.5 

39.5 

13.0 

1300 

486 

195.5 

46.4 

15.2 

1400 

227.0 

53.8 

17.6 

• 

1500 

261.0 

61.8 

20.3 

1600 

296.0 

70.4 

23.1 

1700 

335.0 

79.3 

26.1 

1800 

375.0 

89.0 

29.2 

1900 

418.0 

99.0 

32.5 

2000 

463.0 

110.0 

36.1 

2200 

133.0 

43.6 

2400 

158.0 

52.0 

2600 

186.0 

61.0 

2800 

216.0 

70.6 

3000 

247.5 

81.1 

3200 

284.0 

92.2 

3400 

318.0 

104.0 

3600 

356.0 

117.0 

478 


gg§£  S  g    ?      8 


I'O 


Tp 


M73420 


07 


THE  UNIVERSITY  OF  CALIFORNIA  LIBRARY 


V" 


*   * 


